Antibody purification and purity monitoring

ABSTRACT

Processes for producing and purifying recombinant proteins are disclosed. In particular, the present disclosure provides processes of producing and purifying multi-subunit proteins expressed in yeast or filamentous fungal cells. The production and/or purification of such proteins are monitored for impurities, preferably using lectin binding assays, such that one or more process parameters may be adjusted to maximize the amount of desired recombinant protein and minimize the amount of glycosylated impurities. The processes can also be monitored for other undesired product-associated impurities, such as aggregates and nucleic acids. In exemplary embodiments, the recombinant proteins are multi-subunit proteins, such as antibodies, the host cell is a yeast, such as  Pichia pastoris , and the glycosylated impurity is a glycovariant of the desired recombinant polypeptide, such as an N-linked and/or O-linked glycovariant.

FIELD OF INVENTION

The present disclosure generally relates to processes for producing andpurifying recombinant polypeptides. In particular, the presentdisclosure provides processes of producing and purifying homopolymericor heteropolymeric polypeptides expressed in yeast or filamentous fungalcells using lectin binding assays to monitor for glycosylatedimpurities. As a result, the fermentation process and/or thepurification method may be adjusted to maximize the amount of desiredrecombinant protein and minimize the amount of glycosylated impuritiesand other undesired product-associated impurities, such as aggregatesand nucleic acids. In exemplary embodiments, the recombinant proteinsare multi-subunit proteins, such as antibodies, the host cell is ayeast, such as Pichia pastoris, and the glycosylated impurity is aglycovariant of the desired recombinant polypeptide, such as an N-linkedand/or O-linked glycovariant.

BACKGROUND

Large-scale, economic purification of proteins is an increasinglyimportant concern in the biotechnology industry. Generally, proteins areproduced by cell culture using, prokaryotic, e.g., bacterial, oreukaryotic, e.g., mammalian or fungal, cell lines engineered to producethe protein of interest by insertion of a recombinant plasmid comprisingthe gene for that protein. Since the cell lines used are livingorganisms, they must be fed with a complex growth medium, comprisingsugars, amino acids, and growth factors, sometimes supplied frompreparations of animal serum. Separation of the desired recombinantprotein from the mixture of compounds fed to the cells and from theby-products generated by the cells themselves to a purity sufficient foruse as a human therapeutic poses a formidable challenge.

Multimeric, e.g., homopolymeric and heteropolymeric, proteins representone of the most complex levels of structural organization in biologicalmolecules. Not only do the constituent polypeptide chains have to fold(into secondary structures and tertiary domains) but they must also formcomplementary interfaces that allow stable subunit interactions. Theseinteractions are highly specific and can be between identical subunitsor between different subunits.

In particular, conventional antibodies are tetrameric proteins composedof two identical light chains and two identical heavy chains. Pure humanantibodies of a specific type can be difficult to purify from naturalsources in sufficient amounts for many purposes. As a consequence,biotechnology and pharmaceutical companies have turned to recombinantDNA-based methods to prepare antibodies on a large scale. Hundreds oftherapeutic monoclonal antibodies (mAbs) are either currently on themarket or under development. The production of functional antibodies(including antibody fragments that retain antigen-specificity and oftendisplay improved functionality and physico-chemical properties)generally involves the synthesis of the two polypeptides as well as anumber of post-translational events, including proteolytic processing ofthe N-terminal secretion signal sequence; proper folding and assembly ofthe polypeptides into tetramers; formation of disulfide bonds; andtypically includes a specific N-linked glycosylation.

Additionally, cytokines, as pleiotropic regulators that controlproliferation, differentiation, and other cellular functions of immuneand hematopoictic systems, have potential therapeutic use for a widerange of infectious and autoimmune diseases. Much like antibodies,recombinant expression methods are often used to express recombinantcytokines for subsequent use in research and pharmaceuticalapplications.

Recombinant synthesis of such proteins has typically relied on culturesof higher eukaryotic cells to produce biologically active material, withcultured mammalian cells being very commonly used. However, mammaliantissue culture-based production systems incur significant added expenseand complication relative to microbial fermentation methods.Additionally, products derived from mammalian cell culture may requireadditional safety testing to ensure freedom from mammalian pathogens(including viruses) that might be present in the cultured cells oranimal-derived products used in culture, such as serum.

Prior work has helped to establish the yeast Pichia pastoris as acost-effective platform for producing functional antibodies that arepotentially suitable for research, diagnostic, and therapeutic use. Seeco-owned U.S. Pat. Nos. 7,935,340; 7,927,863 and 8,268,582, each ofwhich is incorporated by reference herein in its entirety. Methods arealso known in the literature for design of P. pastoris fermentations forexpression of recombinant proteins, with optimization having beendescribed with respect to parameters including cell density, brothvolume, substrate feed rate, and the length of each phase of thereaction. See Zhang et al., “Rational Design and Optimization ofFed-Batch and Continuous Fermentations” in Cregg, J. M., Ed., 2007.Pichia Protocols (2nd edition), Methods in Molecular Biology, vol. 389,Humana Press. Totowa, N.J., pgs. 43-63. See also, US 20130045888,entitled MULTI-COPY STRATEGY FOR HIGH-TITER AND HIGH-PURITY PRODUCTIONOF MULTI-SUBUNIT PROTEINS SUCH AS ANTIBODIES IN TRANSFORMED MICROBESSUCH AS PICHIA PASTORIS; and US 20120277408, entitled HIGH-PURITYPRODUCTION OF MULTI-SUBUNIT PROTEINS SUCH AS ANTIBODIES IN TRANSFORMEDMICROBES SUCH AS PICHIA PASTORIS.

Though recombinant proteins can be produced from cultured cells,undesired side-products may also be produced. For example, the culturedcells may produce the desired protein along with proteins havingundesired or aberrant glycosylation. Additionally, cultured cells mayproduce multi-subunit protein along with free monomers and complexeshaving incorrect stoichiometry. Purification of the desiredmulti-subunit protein can increase production cost, and the stepsinvolved in purification may decrease total yield of the desiredcomplex. Moreover, even after purification, undesired side-products maybe present in amounts that cause concern. For example, glycosylatedside-products may be present in amounts that increase the risk of animmune reaction after administration, and may adversely affectproperties such as stability, half-life, and specific activity, whereasaberrant complexes or aggregates may decrease specific activity and mayalso be potentially immunogenic.

SUMMARY

The invention provides a process for purifying a desired recombinantpolypeptide from one or more samples resulting from a fermentationprocess that comprises culturing a desired cell or microbe underconditions that result in the expression and secretion of therecombinant polypeptide and one or more impurities into the fermentationmedium; wherein the purification process includes detecting the amountand/or type of glycosylated impurities in the sample(s) using a lectinthat binds to said glycosylated impurities, such as a glycovariant ofthe desired recombinant polypeptide resulting from, e.g., O-linkedglycosylation and/or N-linked glycosylation.

In one embodiment, the purification process optionally further comprisescontacting the sample(s) with at least one chromatographic support andselectively eluting the desired recombinant polypeptide, and detectingthe amount and/or type of glycosylated impurities in the eluate orfractions thereof using a lectin that binds to said glycosylatedimpurities. The detection step can be effected using at least one lectinselected from ConA, LCH, GNA or GNL, RCA, DC-SIGN, L-SIGN, PNA, AIL,VVL, WGA, SNA, MAL, MAH, UEA and AAL. See Table 3. Preferably, thelectin is bound to a support. In one embodiment, the detection step usesa protein-protein interaction monitoring process, such as, but notlimited to, light interferometry (ForteBio Octet®), dual polarizationinterferometry (Farfield AnaLight®), static light scattering (WyattDynaPro NanoStari™), dynamic light scattering (Wyatt DynaPro NanoStar™),multi-angle light scattering (Wyatt Calypso II), surface plasmonresonance (ProteOn XPR36 or Biacore T100), ELISA, chemiluminescentELISA, far western, electrochemiluminescence (such as that done using aMesoScale Discovery) or other lectin kinetic binding assay.

In one embodiment, the desired recombinant polypeptide is ahomopolymeric or heteropolymeric polypeptide. Such homopolymeric orheteropolymeric recombinant polypeptides include, but are not limitedto, hormones, growth factors, receptors (e.g., GPCRs and immune cellreceptors), antibodies, cytokines, receptor ligands, transcriptionfactors, toxins or enzymes. Non-limiting exemplary antibodies orantibody fragments include those that specifically bind to IL-2, IL-4,IL-6, IL-10. IL-12, IL-13, IL-17, IL-18. IFN-alpha. IFN-gamma, BAFF,CXCL13, IP-10, CBP, angiotensin (angiotensin I and angiotensin II),Nav1.7, Nav1.8, VEGF, PDGF, EPO, EGF, FSH, TSH, hCG, CGRP, NGF, TNF,HGF, BMP2. BMP7, PCSK9 or HRG. Preferably, the desired recombinantpolypeptide is an antibody or an antibody fragment. In anotherembodiment, the antibody or antibody fragment is a human antibody or ahumanized antibody or fragment thereof. The humanized antibody can be ofmouse, rat, rabbit, goat, sheep, or cow origin. Preferably, thehumanized antibody is of rabbit origin. In yet another embodiment, theantibody or antibody fragment comprises a monovalent, bivalent, ormultivalent antibody.

In one embodiment, the desired recombinant polypeptide is expressed in ahost cell that is a yeast or filamentous fungi. The yeast can beselected from Arxiozyma; Ascoboloyma; Citeromyces; Debaryomyces;Dekkera; Eremothecium; Issatchenkia; Kazachstania; Kluvveronmvces;Kodacmraea; Lodderormyces; Pachysolen; Pichia; Saccharomyces;Saturnispora; Tetrapisispora; Torulaspora; Williopsis;Zvgosaccharomyces; Yarrowia; Rhodosporidiunm; Candida; Hansenula;Filobasium; Spxridiobolus; Bullera; Leucosporidium and Filobasidella.Preferably, the yeast is Pichia pastoris, Pichia angusta, Pichiaguillermordii, Pichia melnaiolica, or Pichia inositovera. Morepreferably, the yeast is Pichia pastoris. In a preferred embodiment thePichia pastoris expresses an antibody or antibody fragment. Thefilamentous fungi can be selected from Aspergillus, Tricholerma,Penicillium, Rhizopus, Paecilomyces, Fusarium, Neurospora and Claviceps.

In one embodiment, the purification process includes chromatographicpurification of the desired recombinant polypeptide comprising: (a)contacting the sample(s) with an affinity chromatographic support andseparating the desired recombinant polypeptide from the support; (b)contacting the eluate or fraction thereof of step (a) with a mixed modechromatographic support and selectively eluting the desired recombinantpolypeptide from the support; and (c) contacting the eluate or fractionthereof of step (b) with a hydrophobic interaction chromatographicsupport and selectively eluting the desired recombinant polypeptide fromthe support, wherein the cluate or fraction thereof of step (c)comprises substantially purified desired recombinant polypeptide. In oneembodiment, the affinity chromatographic support comprises animmunoaffinity ligand, such as Protein A, e.g., MabSelect SuRe, orlectin. e.g., GNL or DC-SIGN. A buffer comprising about 1 M arginine, pH4.0 can be applied to the chromatographic support to elute the desiredmulti-subunit complex. In another embodiment, the mixed modechromatographic support is ceramic hydroxyapatite. A buffer comprisingabout 5 mM sodium phosphate, pH 6.5, and about 0 M to about 1.5 M sodiumchloride can be applied to the chromatographic support to elute thedesired recombinant polypeptide. Alternatively, a buffer comprisingabout 5 mM to about 0.25 M sodium phosphate, pH 6.5, can be applied tothe chromatographic support to elute the desired recombinant polypeptide

In yet another embodiment, the hydrophobic interaction chromatographicsupport is polypropylene glycol (PPG) 600 M. A buffer comprising fromabout 0.7 M to 0 M sodium sulfate in about 20 mM sodium phosphate. pH7.0 can be applied to the chromatographic support to elute the desiredrecombinant polypeptide.

Preferably, the eluate or fraction thereof from at least one of step(a), step (b) and step (c) is contacted with the lectin to detect theamount and/or type of glycosylated impurities in the eluate or fractionthereof. Different samples or eluates or fractions thereof containingthe desired recombinant polypeptide can be pooled based on the amountand/or type of detected glycosylated impurity. For example, differentsamples or eluates or fractions thereof containing the desiredrecombinant polypeptide are pooled based on the amount and/or type ofdetected glycosylated impurity relative to the amount of recombinantpolypeptide. In one embodiment, samples or eluate or fractions thereofcomprising less than 10% glycovariant, less than 5% glycovariant, lessthan 1% glycovariant, or less than 0.5% glycovariant are pooled.Additionally, different samples or eluate or fractions thereof can bepooled based on the purity of the desired recombinant polypeptide. Forexample, samples or eluate or fractions thereof comprising greater than91% purity, greater than 97% purity, or greater than 99% purity arepooled. In one embodiment, the purity is determined by measuring themass of glycosylated heavy chain polypeptide and/or glycosylated lightchain polypeptide as a percentage of total mass of heavy chainpolypeptide and/or light chain polypeptide. In a preferred embodiment,the eluate of step (c) comprises less than 50 ng/mg of glycovariant;more preferably, the eluate of step (c) comprises less than 25 ng/mg ofglycovariant; most preferably, the eluate of step (c) comprises lessthan 10 ng/mg of glycovariant. In another preferred embodiment, theeluate of step (c) comprises lectin activity ranging from about 0.2 toabout 2 relative Units (RU) as measured by a lectin binding kineticassay; more preferably, the eluate of step (c) comprises less than 10ng/mg of fungal cell protein. In yet another preferred embodiment, theeluate of step (c) comprises less than 5 ng/mg of a fungal cell protein;more preferably, the eluate of step (c) comprises less than 2 ng/mg of afungal cell protein. In yet a further preferred embodiment, the eluateof step (c) comprises less than 10 ng/mg of nucleic acid; morepreferably, the eluate of step (c) comprises less than 5 ng/mg ofnucleic acid.

In another embodiment, certain samples or eluate or fractions thereofare discarded based on the amount and/or type of detected glycosylatedimpurities. In yet another embodiment, certain samples or fractions aretreated to reduce and/or remove the glycosylated impurities based on theamount and/or type of detected glycosylated impurities. Exemplarytreatments include one or more of the following: (i) addition of anenzyme or other chemical moiety that removes glycosylation. (ii) removalof the glycosylated impurities by effecting one or more lectin bindingsteps, (iii) effecting size exclusion chromatography to remove theglycosylated impurities.

In particular, the invention provides a process for purifying a desiredrecombinant polypeptide expressed in a fungal cell, preferably Pichiapastoris, from a mixture comprising the desired polypeptide and at leastone glycosylated impurity, the purification process comprising: (a)contacting the mixture with an affinity chromatographic support andselectively eluting the multi-subunit protein from the support; (b)contacting the eluate or a fraction thereof of step (a) with a mixedmode chromatographic support and selectively eluting the multi-subunitprotein from the support; and (c) contacting the eluate or a fractionthereof of step (b) with a hydrophobic interaction chromatographicsupport and selectively eluting the multi-subunit protein from thesupport, wherein the eluate or a fraction thereof of step (c) comprisessubstantially purified desired recombinant polypeptide. The amountand/or type of glycosylated impurities in the eluate or a fractionthereof of step (b) and/or step (c) is detected using a lectin thatbinds to said glycosylated impurities and one or more fractions of theeluate of step (b) and/or step (c) is selected for further processingbased on the detected amount and/or type of glycosylated impurities.Preferably, the affinity chromatographic support is a Protein A columnand/or the mixed mode chromatographic support is a hydroxyapatite columnand/or the hydrophobic interaction chromatographic support is a PPG-600Mcolumn. Alternatively, the affinity chromatographic support is a lectincolumn.

In one embodiment, the desired recombinant polypeptide is amulti-subunit protein, preferably an antibody. In another embodiment,the detection step is effected using at least one lectin selected fromConA, LCH, GNA, RCA, DC-SIGN, L-SIGN, PNA, AIL, VVL, WGA, SNA. MAL, MAH,UEA and AAL in a protein-protein interaction monitoring process selectedfrom light interferometry (ForteBio Octet®), dual polarizationinterferometry (Farfield AnaLight®), static light scattering (WyattDynaPro NanoStar™), dynamic light scattering (Wyatt DynaPro NanoStar™),multi-angle light scattering (Wyatt Calypso II), surface plasmonresonance (ProteOn XPR36 or Biacore T100), ELISA, chemiluminescentELISA, far western, electrochemiluminescence (such as that done using aMesoScale Discovery) or other lectin kinetic binding assay. Preferably,the detection step is effected using GNA (or GNL) and/or DC-SIGNlectin(s) in a light interferometry (ForteBio Octet®) assay.

The invention further provides a fermentation process for producing adesired recombinant polypeptide and purifying the desired recombinantpolypeptide from the fermentation medium. The process includes: (i)culturing a host cell or microbe under conditions that result in theexpression and secretion of the recombinant polypeptide and one or moreimpurities into the fermentation medium; (ii) periodically obtaining oneor more samples of the fermentation medium as the fermentation processproceeds or after different fermentation runs are conducted; (iii)detecting the amount and/or type of glycosylated impurities in thesample(s) using a lectin that binds to said glycosylated impurities, and(iv) based on the amount of detected glycosylated impurities in thesample(s) modifying one or more of the operating parameters orconditions of the fermentation process. The glycosylated impurity can bea glycovariant of the recombinant polypeptide, preferably the result ofO-linked glycosylation and/or N-linked glycosylation.

In one embodiment, the detection step is effected using at least onelectin, preferably a lectin bound to a support, selected from ConA, LCH,GNA, RCA, DC-SIGN, L-SIGN, PNA, AlL, VVL, WGA, SNA, MAL, MAH, UEA andAAL. In another embodiment, the detection step uses a protein-proteininteraction monitoring process, such as light interferometry (ForteBioOctet®), dual polarization interferometry (Farfield AnaLight®), staticlight scattering (Wyatt DynaPro NanoStar™), dynamic light scattering(Wyatt DynaPro NanoStar™), composition-gradient multi-angle lightscattering (Wyatt Calypso II), surface plasmon resonance (ProteOn XPR36or Biacore T100). ELISA, chemiluminescent ELISA, far western,electrochemiluminescence (such as that done using a MesoScale Discovery)or other lectin kinetic binding assay.

In one embodiment, based on the amount of glycosylated impuritiesdetected one or more of the following parameters or conditions of thefermentation process are altered: temperature, pH, gas constituent, feedconstituent, agitation, aeration, antifoam and duration.

In another embodiment, the recombinant polypeptide is a homopolymeric orheteropolymeric polypeptide. Exemplary recombinant multimericpolypeptide include a hormone, growth factor, receptor, antibody,cytokine, receptor ligand, transcription factor or enzyme. Preferably,the recombinant polypeptide is an antibody or antibody fragment.Exemplary antibodies and antibody fragments include those thatspecifically bind to IL-2, IL-4, IL-6, IL-10, IL-12, IL-13, IL-17,IL-18, IFN-alpha, IFN-gamma, BAFF, CXCL13, IP-10, CBP, angiotensin(angiotensin I and angiotensin II), Nav1.7, Nav1.8, VEGF, PDGF, EPO,EGF, FSH, TSH, hCG, CGRP. NGPF, TNF, HGF, BMP2, BMP7, PCSK9 or HRG. Inone embodiment, the antibody or antibody fragment is a human antibody ora humanized antibody or fragment thereof. The humanized antibody can beof mouse, rat, rabbit, goat, sheep, or cow origin. Preferably, thehumanized antibody is of rabbit origin. In one embodiment, the antibodyor antibody fragment comprises a monovalent bivalent, or multivalentantibody.

In one embodiment, the host cell is a yeast or filamentous fungi.Preferably, the yeast host cell is selected from Arxiozyma;Ascobolryozvma; Citeromyces; Debaryomytces; Dekkera; Eremothecium;Isatchenkia; Kazachstania; Kluwveromces; Kodamaea; Lodderomyces;Pachvsolen; Pichia; Saccharomyces; Saturnispora; Tetrapisispora;Torulaspora; Williopsis; Zygosaccharomyces; Yarrowia; Rhodosporidium;Candida; Hansenula; Filobasium; Sporidiobolus; Bullera; Leucosporidiumand Filobasidella. More preferably, the yeast host cell is Pichiapastoris, Pichia angusta, Pichia guillermordii, Pichia nmetanolica, orPichia inositovera. Most preferably, the yeast host cell is Pichiapastoria. In a preferred embodiment, the Pichia pastoris expresses anantibody or antibody fragment. In an alternate embodiment, thefilamentous fungal host cell is selected from Aspergillus, Trichoderma,Penicillium, Rhizopus, Paecilomyces, Fusarium, Neurspora and Claviceps.

In another embodiment, the process further includes recovering orpurifying the recombinant polypeptide from the fermentation medium.Preferably, the purification process further comprises contacting thesample(s) with at least one chromatographic support and selectivelyeluting the desired recombinant polypeptide. In one embodiment, thepurification process further comprises pooling different samples oreluates or fractions thereof containing the desired recombinantpolypeptide based on the amount and/or type of detected glycosylatedimpurity. For example, different samples or eluates or fractions thereofcontaining the desired recombinant polypeptide can be pooled based onthe amount and/or type of detected glycosylated impurity relative to theamount of recombinant polypeptide.

In one embodiment, the process further comprises detecting the amount ofaggregated and/or disaggregated impurities in the samples or fractionsusing size exclusion chromatography. Preferably, based on the amount ofaggregated and/or disaggregated impurities detected, one or more of thefollowing parameters or conditions of the fermentation process arealtered: temperature, pH, gas constituent, feed constituent, agitation,aeration, antifoam and duration.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 provides an overview of an exemplary methodology for purificationof monoclonal antibodies expressed in transformed cells, such as Pichia,from product-associated impurities, including monitoring the presence ofimpurities throughout the purification process.

FIG. 2 graphically illustrates lectin binding to a glycosylated protein.Lectin kinetic binding assays (such as light interferometry) areillustrated for use in an analytical technique to monitor thepurification of a main product, e.g., antibody, from glycosylatedimpurities.

FIG. 3 graphically illustrates the presence of glycosylated variants,including O-linked glycosylated products, associated with the productionof proteins in Pichia. Fractions from hydroxyapatite chromatographicseparation of Ab-A were analyzed for the amount of glycosylated productspresent using an immobilized lectin (GNA. Snowdrop) in an Octetinstrument.

FIG. 4A-B graphically illustrates that the level of glycosylatedimpurities determined by lectin kinetic binding assays correlate withthe level of glycosylated impurities determined by size exclusionchromatography. The abbreviation GV refers to glycovariant. Lectinbinding response data from Octet assays (RU) for GNA and DC-SIGN inhydroxyapatite chromatography fractions of Ab-A (Fraction 1-Fraction 21)are graphed with the percent glycovariant as determined by sizeexclusion (SE)-HPLC of the same fractions. See. FIG. 4A. A sampleSE-HPLC chromatograph shows separation of glycovariant from IgG. The GVpeak, which eluted at 15.9 minutes at room temperature) is marked withan arrow. The IgG peak eluted at 17.2 minutes at room temperature.

FIG. 5A-B shows the glycosylated impurity content of hydroxyapatitechromatography fractions of Ab-A produced in Pichia, which was used todetermine which fractions to pool for further purification. For example,two pools were delineated based on different stringencies: BaselinePooling Criteria—pool fractions with ≥91% purity and ≤5.0% variant(Fraction 1-Fraction 13); and Stringent Pooling Criteria—pool fractionswith ≤1.0% variant (Fraction 1-Fraction 10). See, FIG. 5A. Theabbreviation GV refers to glycovariant. SE-HPLC data shows that theBaseline Pool (Fraction 1-Fraction 13) has 0.4% GV, whereas theStringent Pool (Fraction 1-Fraction 10) has 0.1% GV. O-glyco analysis(mol sugar/mol mAb) of the pools shows reduced monomannose andmannotriose in the Stringent Pool as compared to the Baseline Pool(i.e., 1.55 mol monomannose/mol Ab-A in the Stringent Pool compared to1.60 mol monomannose/mol Ab-A in the Baseline Pool, and 0.22 molmannotriose/mol Ab-A in the Stringent Pool compared to 0.28 molmannotriose/mol Ab-A in the Baseline Pool). GNA-Octet response data (RU)confirmed reduced levels ofglycovariants in the Stringent Criteria Poolcompared to the Baseline Pool (i.e., 1.9 RU versus 2.3 RU,respectively). See, FIG. 58.

FIG. 6A-B shows the glycosylated impurity content of hydrophobicinteraction chromatography fractions of Ab-A produced in Pichia, whichwas used to determine which fractions to pool for further purification.For example, two possible pools were delineated based on differentstringencies: Baseline Pooling Criteria—pool from first fraction with≥97% purity on front flank to last fraction with ≥99% purity on rearflank (Fraction 4-Fraction 23); and Stringent Pooling Criteria—pool fromfirst fraction with ≤10 RU GNA activity on front flank to last fractionwith ≥99% SE-HPLC purity on rear flank (Fraction 8-Fraction 23). See,FIG. 6A. The abbreviation GV refers to glycovariant. The abbreviationLMW refers to low molecular weight impurities. SE-HPLC data shows thatthe Baseline Pool (Fraction 4-Fraction 23) has 0.4% GV, whereas theStringent Pool (Fraction 8-Fraction 23) has 0.3% GV. O-glyco analysis(mol sugar/mol mAb) of the pools shows reduced monomannose, mannobioseand mannotriose in the Stringent Pool as compared to the Baseline Pool(i.e., 1.57 mol monomannose/mol Ab-A in the Stringent Pool compared to1.48 mol monomannose/mol Ab-A in the Baseline Pool; 0.52 molmannobiose/mol Ab-A in the Stringent Pool compared to 0.14 molmannobiose mol/Ab-A mol in the Baseline Pool; and 0.32 molmannotriose/mol Ab-A in the Stringent Pool compared to 0.07 molmannotriose/mol Ab-A in the Baseline Pool). GNA-Octet data confirmedreduced levels of glycovariants in the Stringent Criteria Pool comparedto the Baseline Pool (i.e., 1.1 RU versus 1.4 RU, respectively). See,FIG. 6B.

FIG. 7A-B shows stained SDS-PAGE gels run under non-reducing andreducing conditions (FIG. 7 panel A and panel B, respectively) of Ab-Aproduced in Pichia. Purification is observed as reduced levels ofproduct-related impurities in processing from Protein A eluate to CHTpool to PPG HIC pool. In both panels; Lanes 1 and 12: control lanes (Xsample buffer); lanes 2, 6 and 11: molecular weight markers; lanes 3-5:total sample loaded onto the Protein A affinity column; lane 7: Ab-Aantibody preparation after Protein A affinity chromatography; lane 8:Ab-A antibody preparation after ClHIT chromatography; lane 9; Ab-Aantibody preparation after HIC chromatography; and lane 10: Ab-Aantibody preparation after bulk filtration (BDS).

FIG. 8 shows a reduction in glycovariant (GV) impurities duringdownstream purification of Ab-B as monitored using the GNA lectin assay.

FIG. 9 shows a separation of glycovariant (GV) impurities during HICpurification of Ab-B. Pools of fractions from the HIC elution weretested for GV content using the GNA lectin assay. Fractions from thefront of the elution peak (fraction 1-fraction 5) and fractions from therear of the elution peak (fraction 26-fraction 32) has higher lectinactivity than fractions from the middle of the peak (fraction 6-fraction25). Also, fraction 6-fraction 25 contained the desired purified Ab-Bproduct.

FIG. 10 shows stained SDS-PAGE gels run under non-reducing and reducingconditions (FIG. 10 panel A and panel B, respectively) of Ab-B producedin Pichia. Purification is observed as reduced levels of product-relatedimpurities in processing from Protein A eluate to CHT pool to Phenyl HPHIC pool. In both panels: lanes 1, 2 and 6 contain molecular weightmarkers; lane 3 contains Protein A eluate; lane 4 contains CHT pool; andlane 5 contains HIC pool

DETAILED DESCRIPTION

The present disclosure provides processes for producing and purifyingrecombinant polypeptides expressed by a host cell or microbe. Inparticular, the present disclosure provides processes of producing andpurifying homopolymeric or heteropolymeric polypeptides, such anantibodies, expressed in yeast or filamentous fungal cells. The presentmethods incorporate lectin binding as a quantitative indicator ofglycosylated impurities, such that the production and/or purificationprocess can be modified to maximize the yield of the desired protein anddecrease the presence of glycosylated impurities.

Additionally, the present processes encompass purification processescomprising chromatographic separation of samples from the fermentationprocess in order to substantially purify the desired recombinantpolypeptide from undesired product-associated impurities, such asglycosylated impurities (e.g., glycovariants), nucleic acids andaggregates/disaggregates. In some embodiments, the eluate or fractionsthereof from different chromatography steps are monitored for lectinbinding activity to detect the type and/or amount of glycosylatedimpurities. Based on the amount and/or type of glycosylated impuritiesdetected, certain samples from the fermentation process and/or fractionsfrom the chromatographic purification are discarded, treated and/orselectively pooled for further purification.

In exemplary embodiments, the recombinant protein is an antibody or anantibody binding fragment, the yeast cell is Pichia pastoris, and theglycosylated impurity is a glycovariant of the desired recombinantpolypeptide, such as an N-linked and/or O-linked glycovariant.

In a preferred embodiment, the recombinant protein is an antibody orantibody fragment, such as a humanized or human antibody, comprised oftwo heavy chain subunits and two light chain subunits. Preferred fungalcells include yeasts, and particularly preferred yeasts includemethylotrophic yeast strains, e.g., Pichia pastoris, Hansenulapolymorpha (Pichia angusta), Pichia guillermordii, Pichia methanolica,Pichia inositovera, and others (see. e.g., U.S. Pat. No. 4,812,405,4,818,700, 4,929,555, 5,736,383, 5,955,349, 5,888,768, and 6,258,559each of which is incorporated by reference in its entirety). The yeastcell may be produced by methods known in the art. For example, a panelof diploid or tetraploid yeast cells containing differing combinationsof gene copy numbers may be generated by mating cells containing varyingnumbers of copies of the individual subunit genes (which numbers ofcopies preferably are known in advance of mating).

Applicants have discovered novel processes for the production andpurification of proteins produced in yeast or filamentous fungal cellsthat provides a high yield of the desired protein with minimalimpurities. In particular, the processes disclosed herein incorporatepurity monitoring steps into the protein production and/or purificationschemes to improve the removal of product-associated impurities, e.g.,glycosylated impurities, from the main protein product of interest,e.g., by selectively discarding, treating and/or purifying certainfractions from the production and/or purification schemes based on theamount and/or type of detected glycosylated impurity relative to theamount of recombinant polypeptide. The working examples demonstrate thatemploying such production and purification monitoring methods results inhigh levels of product purification (e.g., at least 97% purity) whilemaintaining a high yield of the desired protein product.

In one embodiment, the methods include a fermentation process forproducing a desired recombinant polypeptide and purifying the desiredrecombinant polypeptide from the fermentation medium. Generally, a yeastcell or microbe is cultured under conditions resulting in expression andsecretion of the recombinant polypeptide as well as one or moreimpurities into the fermentation medium, a sample is collected, e.g.,during or after the fermentation run, and the amount and/or type ofglycosylated impurities in the sample(s) is monitored using a lectin,such that parameters of the fermentation process, e.g., temperature, pH,gas constituents (e.g., oxygen level, pressure, flow rate), feedconstituents (e.g., glucose level or rate), agitation, aeration,antifoam (e.g., type or concentration) and duration, can be modifiedbased on the detected glycosylated impurities.

In another embodiment, the methods include a process for purifying adesired recombinant polypeptide from one or more samples, which resultfrom a fermentation process that comprises culturing a desired cell ormicrobe under conditions that result in the expression and secretion ofthe recombinant polypeptide and one or more impurities into thefermentation medium, by using lectin binding to detect the amount and/ortype of glycosylated impurities in the sample(s). The inventors havedetermined that lectin kinetic binding assays provide a quantitativemeasure of glycosylated impurities, such that the purification processcan be adjusted in response to the detected level and type of impurity.

In a particular embodiment, the purification process further includescontacting one or more samples from the fermentation process, e.g.,fermentation medium containing the desired recombinant protein, e.g., anantibody, expressed in a host yeast or filamentous fungal cell and animpurity, with at least one chromatographic support and then selectivelyeluting the desired recombinant polypeptide. For example, thefermentation process sample may be tested for the glycosylatedimpurities using a kinetic lectin binding assay and, depending on thetype and/or amount of glycosylated impurities detected, contacted withan affinity chromatographic support (e.g., Protein A or lectin), a mixedmode chromatographic support (e.g., ceramic hydroxyapatite) and ahydrophobic interaction chromatographic support (e.g., polypropyleneglycol (PPG) 600M). The desired protein is separated, e.g., selectivelyeluted, from each chromatographic support prior to being contacted withthe subsequent chromatographic support, resulting in the eluate or afraction thereof from hydrophobic interaction chromatographic supportcomprising a substantially purified desired recombinant protein.

“Substantially purified” with regard to the desired protein ormulti-subunit protein means that the sample comprises at least 90%, atleast 91%, at least 92%, at least 93%, at least 94%, at least 95%, atleast 96%, at least 97%, at least 98%, or at least 98.5% of the desiredrecombinant protein with less than 3%, less than 2.5%, less than 2%,less than 1.5% or less than 1% of impurities. i.e., aggregate, variantand low molecular weight product. In one embodiment, the substantiallypurified protein comprises less than 50 ng/mg, preferably less than 25ng/mg or more preferably less than 10 ng/mg of glycovariant; less than10 ng/mg, preferably less than 5 ng/mg or more preferably less than 2ng/mg of fungal cell protein; and/or less than 10 ng/mg or preferablyless than 5 ng/mg of nucleic acid.

The methods optionally further include monitoring a sample of thefermentation process and/or a portion of the eluate or a fractionthereof from at least one of the affinity chromatographic support, themixed mode chromatographic support and the hydrophobic interactionchromatographic support for the presence of at least oneproduct-associated impurity, such as a fungal cell protein, a fungalcell nucleic acid, an adventitious virus, an endogenous virus, anendotoxin, an aggregate, a disaggregate, or an undesired proteincomprising at least one modification relative to the desired recombinantprotein (e.g., an amino acid substitution, N-terminal modification,C-terminal modification, mismatched S—S bonds, folding, truncation.aggregation, multimer dissociation, denaturation, acetylation, fattyacylation, deamidation, oxidation, carbamylation, carboxylation,formylation, gamma-carboxyglutamylation, glycosylation, methylation,phosphorylation, sulphation, PEGylation and ubiquitination). Inparticular, the production and purification processes may includedetecting the amount of aggregated and/or disaggregated impurities inthe samples or fractions using size exclusion chromatography.

Though much of the present disclosure describes production ofantibodies, the methods described herein are readily adapted to othermulti-subunit complexes as well as single subunit proteins. The methodsdisclosed herein may readily be utilized to improve the yield and/orpurity of any recombinant multi-subunit complex comprising two or moredifferent subunits. Additionally, the present methods are not limited toproduction of multi-protein complexes but may also be readily adaptedfor use with ribonucleoprotein (RNP) complexes including telomerase,hnRNPs, ribosomes, snRNPs, signal recognition particles, prokaryotic andeukaryotic RNase P complexes, and any other complexes that containmultiple distinct protein and/or RNA subunits. The fungal cell thatexpresses the multi-subunit complex may be produced by methods known inthe art. For example, a panel of diploid or tetraploid yeast cellscontaining differing combinations of gene copy numbers may be generatedby mating cells containing varying numbers of copies of the individualsubunit genes (which numbers of copies preferably are known in advanceof mating).

Expression of Recombinant Proteins

Recombinant proteins, including homopolymeric or heteropolymericpolypeptides, e.g., an antibody or an antibody fragment, can beexpressed in yeast and filamentous fungal cells. In one embodiment, thedesired protein is recombinantly expressed in yeast, and particularlypreferred yeasts include methylotrophic yeast strains. e.g., Pichiapastoris. Hansenula polyrmorpha (Pichia angusta), Pichia guillermordii,Pichia methanolica, Pichia inositovera, and others (see, e.g., U.S. Pat.Nos. 4,812,405, 4,818,700, 4,929,555, 5,736,383, 5,955,349, 5,888,768,and 6,258,559 each of which is incorporated by reference in itsentirety). Other exemplary yeast include Arxiozyma; Ascobotlrvzvma;Citeronyces; Debaryomyces; Dekkera; Eremothecium; Issatchenkia;Kazachsania; Kluyveromyces; Kodamaea; Lodderomyces; Pachysolen; Pichia;Saccharomyces; Saturnispora; Tetrapisispora; Torulaspora; Williopsis;Zygosaccharomyes; Yarrowia; Rhodsporidium; Candida; Hansenula;Filobasium; Sporidiobolus; Bullera; Leucosporidium and Filobasidella.

The yeast cell may be produced by methods known in the art. For example,a panel of diploid or tetraploid yeast cells containing differingcombinations of gene copy numbers may be generated by mating cellscontaining varying numbers of copies of the individual subunit genes(which numbers of copies preferably are known in advance of mating).

In one embodiment, the yeast cell may comprise more than one copy of oneor more of the genes encoding the recombinant protein or subunits of thedesired multi-subunit protein. For example, multiple copies of a subunitgene may be integrated in tandem into one or more chromosomal loci.Tandemly integrated gene copies are preferably retained in a stablenumber of copies during culture for the production of the desiredprotein or multi-subunit complex. For example, in prior work describedby the present applicants, gene copy numbers were generally stable forP. pastoris strains containing three to four tandemly integrated copiesof light and heavy chain antibody genes (see. U.S. 20130045888).

One or more of the genes encoding the recombinant protein subunits arepreferably integrated into one or more chromosomal loci of a fungalcell. Any suitable chromosomal locus may be utilized for integration,including intergenic sequences, promoters sequences, coding sequences,termination sequences, regulatory sequences, etc. Exemplary chromosomalloci that may be used in P. pastoris include PpURA5; OCH1; AOX1; HIS4;and GAP. The encoding genes may also be integrated into one or morerandom chromosomal loci rather than being targeted. In preferredembodiments, the chromosomal loci are selected from the group consistingof the pGAP locus, the 3′AOX TT locus and the HIS4 TT locus. Inadditional exemplary embodiments, the genes encoding the heterologousprotein subunits may be contained in one or more extrachromosomalelements, for example one or more plasmids or artificial chromosomes.

In exemplary embodiments, the protein may be a multi-subunit proteinthat, e.g., comprises two, three, four, five, six, or more identicaland/or non-identical subunits. Additionally, each subunit may be presentone or more times in each multi-subunit protein. For example, themulti-subunit protein may be a multi-specific antibody such as abi-specific antibody comprising two non-identical light chains and twonon-identical heavy chains. A panel of diploid or tetraploid yeast cellscontaining differing combinations of gene copy numbers may be quicklygenerated by mating cells containing varying copy numbers of theindividual subunit genes. Antibody production from each strain in thepanel may then be assessed to identify a strain for further use based ona characteristic such as yield of the desired multi-subunit protein orpurity of the desired multi-subunit protein relative to undesiredside-products.

The subunits of a multi-subunit may be expressed from monocistronicgenes, polycistronic genes, or any combination thereof. Eachpolycistronic gene may comprise multiple copies of the same subunit, ormay comprise one or more copies of each different subunit.

Exemplary methods that may be used for manipulation of Pichiapatoris(including methods of culturing, transforming, and mating) are disclosedin Published Applications including U.S. 20080003643, U.S. 20070298500,and U.S. 20060270045, and in Higgins, D. R., and Cregg, J. M., Eds.1998. Pichia Protocols. Methods in Molecular Biology. Humana Press,Totowa, N.J., and Cregg, J. M., Ed., 2007, Pichia Protocols (2ndedition), Methods in Molecular Biology. Humana Press, Totowa, N.J., eachof which is incorporated by reference in its entirety.

An exemplary expression cassette that may be utilized is composed of theglyceraldehyde dehydrogenase gene (GAP gene) promoter, fused tosequences encoding a secretion signal, followed by the sequence of thegene to be expressed, followed by sequences encoding a P. pastoristranscriptional termination signal from the P. pastoris alcohol oxidaseI gene (AOX1). The Zeocin resistance marker gene may provide a means ofenrichment for strains that contain multiple integrated copies of anexpression vector in a strain by selecting for transformants that areresistant to higher levels of Zeocin. Similarly, G418 or Kanamycinresistance marker genes may be used to provide a means of enrichment forstrains that contain multiple integrated copies of an expression vectorin a strain by selecting for transformants that are resistant to higherlevels of Geneticin or Kanamycin.

Yeast strains that may be utilized include auxotrophic P. pastoris orother Pichia strains, for example, strains having mutations in met1,lys3, ura3 and ade1 or other auxotrophy-associated genes. Preferredmutations are incapable of giving rise to revertants at any appreciablefrequency and are preferably partial or even more preferably fulldeletion mutants. Preferably, prototrophic diploid or tetraploid strainsare produced by mating a complementing sets of auxotrophic strains.

Prior to transformation, each expression vector may be linearized byrestriction enzyme cleavage within a region homologous to the targetgenomic locus (e.g., the GAP promoter sequence) to direct theintegration of the vectors into the target locus in the fungal cell.Samples of each vector may then be individually transformed intocultures of the desired strains by electroporation or other methods, andsuccessful transformants may be selected by means of a selectablemarker, e.g., antibiotic resistance or complementation of an auxotrophy.Isolates may be picked, streaked for single colonies under selectiveconditions and then examined to confirm the number of copies of the geneencoding the desired protein or subunit of the multi-subunit complex(e.g., a desired antibody) by Southern Blot or PCR assay on genomic DNAextracted from each strain. Optionally, expression of the expectedsubunit gene product may be confirmed, e.g., by FACS, Western Blot,colony lift and immunoblot, and other means known in the art.Optionally, haploid isolates are transformed additional times tointroduce additional heterologous genes, e.g., additional copies of thesame subunit integrated at a different locus, and/or copies of adifferent subunit. The haploid strains are then mated to generatediploid strains (or strains of higher ploidy) able to synthesize themulti-protein complex. Presence of each expected subunit gene may beconfirmed by Southern blotting, PCR, and other detection means known inthe art. Where the desired multi-protein complex is an antibody, itsexpression may also be confirmed by a colony lift/immunoblot method(Wung et al. Biotechniques 21 808-812 (1996)) and/or by FACS.

This transformation protocol is optionally repeated to target aheterologous gene into a second locus, which may be the same gene or adifferent gene than was targeted into the first locus. When theconstruct to be integrated into the second locus encodes a protein thatis the same as or highly similar to the sequence encoded by the firstlocus, its sequence may be varied to decrease the likelihood ofundesired integration into the first locus. For example, the sequence tobe integrated into the second locus may have differences in the promotersequence, termination sequence, codon usage, and/or other tolerablesequence differences relative to the sequence integrated into the firstlocus.

Transformation of haploid P. pastoris strains and genetic manipulationof the P. pastoris sexual cycle may be performed as described in PichiaProtocols (1998, 2007), supra.

Expression vectors for use in the methods of the invention may furtherinclude yeast specific sequences, including a selectable auxotrophic ordrug marker for identifying transformed yeast strains. A drug marker mayfurther be used to amplify copy number of the vector in a yeast cell,e.g., by culturing a population of cells in an elevated concentration ofthe drug, thereby selecting transformants that express elevated levelsof the resistance gene.

The polypeptide coding sequence of interest is typically operably linkedto transcriptional and translational regulatory sequences that providefor expression of the polypeptide in yeast cells. These vectorcomponents may include, but are not limited to, one or more of thefollowing: an enhancer element, a promoter, and a transcriptiontermination sequence. Sequences for the secretion of the polypeptide mayalso be included. e.g. a signal sequence, and the like. A yeast originof replication is optional, as expression vectors are often integratedinto the yeast genome.

In an exemplary embodiment, one or more of the genes encoding theheterologous protein or subunits thereof are coupled to an induciblepromoter. Suitable exemplary promoters include the alcohol oxidase 1gene promoter, formaldehyde dehydrogenase genes (FLD; see U.S. Pub. No.2007/0298500), and other inducible promoters known in the art. Thealcohol oxidase 1 gene promoter, is tightly repressed during growth ofthe yeast on most common carbon sources, such as glucose, glycerol, orethanol, but is highly induced during growth on methanol (Tschopp etal., 1987; U.S. Pat. No. 4,855,231 to Stroman, D. W., et al). Forproduction of foreign proteins, strains may be initially grown on arepressing carbon source to generate biomass and then shifted tomethanol as the sole (or main) carbon and energy source to induceexpression of the foreign gene. One advantage of this regulatory systemis that P. pastoris strains transformed with foreign genes whoseexpression products are toxic to the cells can be maintained by growingunder repressing conditions.

In another exemplary embodiment, one or more of the heterologous genesmay be coupled to a regulated promoter, whose expression level can beupregulated under appropriate conditions. Examples of suitable promotersfrom Pichia include the CUP1 (induced by the level of copper in themedium), tetracycline inducible promoters, thiamine inducible promoters.AOX1 promoter (Cregg et al. (1989) Mol. Cell. Biol. 9:1316-1323); ICL1promoter (Menendez et al. (2003) Yeast 20(13); 1097-108);glyceraldehyde-3-phosphate dehydrogenase promoter (GAP) (Waterham ct al.(1997) Gene 186(1):37-44); and FLD1 promoter (Shen et al. (1998) Gene216(i); 93-102). The GAP promoter is a strong constitutive promoter andthe CUP1, AOX and FLD1 promoters are inducible. Each foregoing referenceis incorporated by reference herein in its entirety.

Other yeast promoters include ADHt, alcohol dehydrogenase II, GAL4,PHO3. PHO5, Pyk, and chimeric promoters derived therefrom. Additionally,non-yeast promoters may be used in the invention such as mammalian,insect, plant, reptile, amphibian, viral, and avian promoters. Mosttypically the promoter will comprise a mammalian promoter (potentiallyendogenous to the expressed genes) or will comprise a yeast or viralpromoter that provides for efficient transcription in yeast systems.

The polypeptides of interest may be produced recombinantly not onlydirectly, but also as a fusion polypeptide with a heterologouspolypeptide. e.g. a signal sequence or other polypeptide having aspecific cleavage site at the N-terminus of the mature protein orpolypeptide. In general, the signal sequence may be a component of thevector, or it may be a part of the polypeptide coding sequence that isinserted into the vector. The heterologous signal sequence selectedpreferably is one that is recognized and processed through one of thestandard pathways available within the fungal cell. The S. cerevisiaealpha factor pre-pro signal has proven effective in the secretion of avariety of recombinant proteins from P. pastoris. Other yeast signalsequences include the alpha mating factor signal sequence, the invertasesignal sequence, and signal sequences derived from other secreted yeastpolypeptides. Additionally, these signal peptide sequences may beengineered to provide for enhanced secretion in diploid yeast expressionsystems. Other secretion signals of interest also include mammaliansignal sequences, which may be heterologous to the protein beingsecreted, or may be a native sequence for the protein being secreted.Signal sequences include pre-peptide sequences, and in some instancesmay include propeptide sequences. Many such signal sequences are knownin the art, including the signal sequences found on immunoglobulinchains, e.g., K28 preprotoxin sequence. PHA-E, FACE, human MCP-I humanserum albumin signal sequences, human Ig heavy chain, human Ig lightchain, and the like. For example, see Hashimoto et. al. Protein Eng11(2) 75 (1998); and Kobayashi et. al. Therapeutic Apheresis 2(4) 257(1998), each of which is incorporated by reference herein in itsentirety.

Transcription may be increased by inserting a transcriptional activatorsequence into the vector. These activators are cis-acting elements ofDNA, usually about from 10 to 300 bp, which act on a promoter toincrease its transcription. Transcriptional enhancers are relativelyorientation and position independent, having been found 5′ and 3′ to thetranscription unit, within an intron, as well as within the codingsequence itself. The enhancer may be spliced into the expression vectorat a position 5′ or 3′ to the coding sequence, but is preferably locatedat a site 5′ from the promoter.

Though optional, in one embodiment, one or more subunit of the desiredprotein or multi-subunit complex is operably linked, or fused, to asecretion sequence that provides for secretion of the expressedpolypeptide into the culture media, which can ticilitate harvesting andpurification of the heterologous protein or multi-subunit complex. Evenmore preferably, the secretion sequences provide for optimized secretionof the polypeptide from the fungal cells (e.g., yeast diploid cells),such as through selecting preferred codons and/or altering thepercentage of AT base pairs through codon selection. It is known in theart that secretion efficiency and/or stability can be affected by thechoice of secretion sequence and the optimal secretion sequence can varybetween different proteins (see. e.g., Koganesawa et al. Protein Eng.2001 September; 14(9):705-10, which is incorporated by reference hereinin its entirety). Many potentially suitable secretion signals are knownin the art and can readily be tested for their effect upon yield and/orpurity of a particular heterologous protein or multi-subunit complex.Any secretion sequences may potentially be used, including those presentin secreted proteins of yeasts and other species, as well as engineeredsecretion sequences. See Hashimoto et al., Protein Engineering vol. 11no. 2 pp. 75-77, 1998; Oka et al., Biosci Biotechnol Biochem. 1999November; 63(11):1977-83; Gellissen et al., FEMS Yeast Research 5 (2005)1079-1096; Ma et al., Hepatology. 2005 December; 42(6):1355-63;Raemackers et al., Eur J Biochem. 1999 Oct. 1; 265(1): 394-403;Koganesawa ct al., Protein Eng. (2001) 14 (9): 705-710; Daly et al.,Protein Expr Purif. 2006 April; 46(2):456-67; Damasceno et al., AppiMicrobiol Iiotechnol (2007) 74:381-389; and Felgenhauer et al., NucleicAcids Res. 1990 Aug. 25:18(16):4927, each of which is incorporated byreference herein in its entirety).

Nucleic acids are “operably linked” when placed into a functionalrelationship with another nucleic acid sequence. For example, DNA for asignal sequence is operably linked to DNA for a polypeptide if it isexpressed as a preprotein that participates in the secretion of thepolypeptide; a promoter or enhancer is operably linked to a codingsequence if it affects the transcription of the sequence. Generally,“operably linked” means that the DNA sequences being linked arecontiguous, and, in the case of a secretory leader, contiguous and inreading frame. However, enhancers do not have to be contiguous. Linkingmay be accomplished by ligation at convenient restriction sites oralternatively via a PCR/recombination method familiar to those skilledin the art (Gateway4 Technology: Invitrogen, Carlsbad Calif.). If suchsites do not exist, the synthetic oligonuclcotide adapters or linkersmay be used in accordance with conventional practice. Desired nucleicacids (including nucleic acids comprising operably linked sequences) mayalso be produced by chemical synthesis.

The protein may also be secreted into the culture media without beingoperably linked or fused to a secretion signal. For example, it has beendemonstrated that some heterologous polypeptides are secreted into theculture media when expressed in P. pastoris even without being linked orfused to a secretion signal. Additionally, the protein may be purifiedfrom fungal cells (which, for example, may be preferable if the proteinis poorly secreted) using methods known in the art.

It is to be understood that this invention is not limited to theparticular methodology, protocols, cell lines, animal species or genera,and reagents described, as such may vary. It is also to be understoodthat the terminology used herein is for the purpose of describingparticular embodiments only, and is not intended to limit the scope ofthe present invention which will be limited only by the appended claims.

As used herein the singular forms “a”, “and”, and “the” include pluralreferents unless the context clearly dictates otherwise. Thus, forexample, reference to “a cell” includes a plurality of such cells andreference to “the protein” includes reference to one or more proteinsand equivalents thereof known to those skilled in the art, and so forth.All technical and scientific terms used herein have the same meaning ascommonly understood to one of ordinary skill in the art to which thisinvention belongs unless clearly indicated otherwise.

As used herein the terms “filamentous fungal cell” and “filamentousfungal host cell” are used interchangeably and are intended to mean anycell from any species from the genera Aspergillus, Trichderma,Penicillium, Rhiropus, Paecilonmyces, Fusarium, Neurospora andClaviceps. In the present invention this is intended to broadlyencompass any filamentous fungal cell that can be grown in culture.

As used herein the term “yeast cell” refers to any cell from any speciesfrom the genera Arxiozyma; Ascobotrozyma; Citerornyces; Debaryomyces;Dekkera; Eremothecium; Issatchenkia; Kazachstania; Kluyveronmvces;Kodamaea; Lodderomyces; Pachysolen; Pichia; Saccharromyces;Saturnispora; Teirapiispora; Torulaspora; Williopsis; Zygosaccharomyces;Yarrowia, Rhodosporidium; Candida; Hansenulda; Filobasium;Sporidiobolus; Bullera; Leucosporidium and Filobasidella. In the presentinvention, this is intended to broadly encompass any yeast cell that canbe grown in culture.

In a preferred embodiment of the invention, the yeast cell is a memberof the genus Pichia or is another methylotroph. In a further preferredembodiment of the invention, the fungal cell is of the genus Pichia isone of the following species: Pichia pastoris, Pichia methanalica, andHansenula polymorpha (Pichia angusta). In a particularly preferredembodiment of the invention, the fungal cell of the genus Pichia is thespecies Pichia pastoris.

Such species may exist in a haploid, diploid, or other polyploid form.The cells of a given ploidy may, under appropriate conditions,proliferate for an indefinite number of generations in that form.Diploid cells can also sporulate to form haploid cells. Sequentialmating can result in tetraploid strains through further mating or fusionof diploid strains. The present invention contemplates the use ofhaploid yeast, as well as diploid or other polyploid yeast cellsproduced, for example, by mating or fusion (e.g., spheroplast fusion).

As used herein “haploid yeast cell” refers to a cell having a singlecopy of each gene of its normal genomic (chromosomal) complement.

As used herein, “polyploid yeast cell” refers to a cell having more thanone copy of its normal genomic (chromosomal) complement.

As used herein. “diploid yeast cell” refers to a cell having two copies(alleles) of essentially every gene of its normal genomic complement,typically formed by the process of fusion (mating) of two haploid cells.

As used herein, “tetraploid yeast cell” refers to a cell having fourcopies (alleles) of essentially every gene of its normal genomiccomplement, typically formed by the process of fusion (mating) of twodiploid cells. Tetraploids may carry two, three, four, or more differentexpression cassettes. Such tetraploids might be obtained in S.cerevisiae by selective mating homozygotic heterothallic a/a andalpha/alpha diploids and in Pichia by sequential mating of haploids toobtain auxotrophic diploids. For example, a [met his] haploid can bemated with [ade his] haploid to obtain diploid [his]: and a [met arg]haploid can be mated with [ade arg] haploid to obtain diploid [arg];then the diploid [his] can be mated with the diploid [arg] to obtain atetraploid prototroph. It will be understood by those of skill in theart that reference to the benefits and uses of diploid cells may alsoapply to tetraploid cells.

As used herein, “yeast mating” refers to the process by which two yeastcells fuse to form a single yeast cell. The fused cells may be haploidcells or cells of higher ploidy (e.g., mating two diploid cells toproduce a tetraploid cell).

As used herein. “meiosis” refers to the process by which a diploid yeastcell undergoes reductive division to form four haploid spore products.Each spore may then germinate and form a haploid vegetatively growingcell line.

As used herein, “folding” refers to the three-dimensional structure ofpolypeptides and proteins, where interactions between amino acidresidues act to stabilize the structure. While non-covalent interactionsare important in determining structure, usually the proteins of interestwill have intra- and/or intermolecular covalent disulfide bonds formedby two cysteine residues. For naturally occurring proteins andpolypeptides or derivatives and variants thereof, the proper folding istypically the arrangement that results in optimal biological activity,and can conveniently be monitored by assays for activity, e.g. ligandbinding, enzymatic activity, etc.

In some instances, for example where the desired product is of syntheticorigin, assays based on biological activity will be less meaningful. Theproper folding of such molecules may be determined on the basis ofphysical properties, energetic considerations, modeling studies, and thelike.

The expression host may be further modified by the introduction ofsequences encoding one or more enzymes that enhance folding anddisulfide bond formation, i.e. foldases, chaperonins, etc. Suchsequences may be constitutively or inducibly expressed in the yeast hostcell, using vectors, markers, etc. as known in the art. Preferably thesequences, including transcriptional regulatory elements sufficient forthe desired pattern of expression, are stably integrated in the yeastgenome through a targeted methodology.

For example, the eukaryotic Protein Disulfide Isomerase (PDI) is notonly an efficient catalyst of protein cysteine oxidation and disulfidebond isomerization, but also exhibits chaperone activity. Co-expressionof PDI can facilitate the production of active proteins having multipledisultide bonds. Also of interest is the expression of BIP(immunoglobulin heavy chain binding protein); cyclophilin; and the like.In one embodiment of the invention, the desired protein or multi-subunitcomplex may be expressed from a yeast strain produced by mating, whereineach of the haploid parental strains expresses a distinct foldingenzyme, e.g. one strain may express BIP, and the other strain mayexpress PDI or combinations thereof.

The terms “desired protein” and “desired recombinant protein” are usedinterchangeably and refer generally to a heterologous protein expressedin a host yeast or filamentous fungal cell comprising a particularprimary, secondary, tertiary and/or quaternary structure with aparticular pattern of post-translational and/or other modifications. Inone aspect, the desired protein is a homopolymeric or heteropolymericmulti-subunit protein. Exemplary multimeric recombinant proteinsinclude, but are not limited to, a multimeric hormone (e.g., insulinfamily, relaxin family and other peptide hormones), growth factor,receptor, antibody, cytokine, receptor ligand, transcription factor orenzyme.

Preferably, the desired recombinant protein is an antibody or anantibody fragment, such as a humanized or human antibody or a bindingportion thereof. In one aspect, the humanized antibody is of mouse, rat,rabbit, goat, sheep, or cow origin. Preferably, the humanized antibodyis of rabbit origin. In another aspect, the antibody or antibodyfragment comprises a monovalent, bivalent, or multivalent antibody. Inyet another aspect, the antibody or antibody fragment specifically bindsto IL-2, IL-4, IL-6, IL-10, IL-12, IL-13, IL-17, IL-18, IFN-alpha,IFN-gamma. BAFF, CXCL13, IP-10, CBP, angiotensin (angiotensin I andangiotensin II). Nav1.7. Nav1.8, VEGF, PDGF, EPO, EGF, FSH, TSH, hCG,CGRP, NGF, TNF, HGF, BMP2, BMP7, PCSK9 or HRG.

The term “antibody” includes any polypeptide chain-containing molecularstructure with a specific shape that fits to and recognizes an epitope,where one or more non-covalent binding interactions stabilize thecomplex between the molecular structure and the epitope. The archetypalantibody molecule is the immunoglobulin, and all types ofimmunoglobulins, IgG, IgM, IgA, IgE, IgD, etc., from all sources, e.g.human, rodent, rabbit, cow, sheep, pig, dog, other mammals, chicken,other avians, etc., are considered to be “antibodies.” A preferredsource for producing antibodies useful as starting material according tothe invention is rabbits. Numerous antibody coding sequences have beendescribed; and others may be raised by methods well-known in the art.Examples thereof include chimeric antibodies, human antibodies and othernon-human mammalian antibodies, humanized antibodies, human antibodies,single chain antibodies such as scFvs, camelbodies, nanobodies. IgNAR(single-chain antibodies derived from sharks), small-modularimmunopharmaceuticals (SMIPs), and antibody fragments such as Fabs.Fab′. F(ab′)₂ and the like. See Streltsov V A, et al., Structure of ashark IgNAR antibody variable domain and modeling of anearly-developmental isotype, Protein Sci. 2005 November; 14(11):2901-9.Epub 2005 Sep. 30; Greenberg A S, et al. A new antigen receptor genefamily that undergoes rearrangement and extensive somaticdiversification in sharks, Nature. 1995 Mar. 9; 374(6518): 168-73;Nuttall S D, et al., Isolation of the new antigen receptor fromwobbegong sharks, and use as a scaffold for the display of protein looplibraries. Mol Immunol. 2001 August: 38(4):313-26; H-lamers-Casterman C,et al., Naturally occurring antibodies devoid of light chains, Nature.1993 Jun. 3: 363(6428):446-8; Gill D S, et al., Biopharmaceutical drugdiscovery using novel protein scaffolds, Curr Opin Biotechnol. 2006December; 17(6):653-8. Epub 2006 Oct. 19. Each foregoing reference isincorporated by reference herein in its entirety.

For example, antibodies or antigen binding fragments may be produced bygenetic engineering. In this technique, as with other methods,antibody-producing cells are sensitized to the desired antigen orimmunogen. The messenger RNA isolated from antibody producing cells isused as a template to make cDNA using PCR amplification. A library ofvectors, each containing one heavy chain gene and one light chain generetaining the initial antigen specificity, is produced by insertion ofappropriate sections of the amplified immunoglobulin cDNA into theexpression vectors. A combinatorial library is constructed by combiningthe heavy chain gene library with the light chain gene library. Thisresults in a library of clones which co-express a heavy and light chain(resembling the Fab fragment or antigen binding fragment of an antibodymolecule). The vectors that carry these genes are co-transfected into ahost cell. When antibody gene synthesis is induced in the transfectedhost, the heavy and light chain proteins self-assemble to produce activeantibodies that can be detected by screening with the antigen orimmunogen.

Antibody coding sequences of interest include those encoded by nativesequences, as well as nucleic acids that, by virtue of the degeneracy ofthe genetic code, are not identical in sequence to the disclosed nucleicacids, and variants thereof. Variant polypeptides can include amino acid(aa) substitutions, additions or deletions. The amino acid substitutionscan be conservative amino acid substitutions or substitutions toeliminate non-essential amino acids, such as to alter a glycosylationsite, or to minimize misfolding by substitution or deletion of one ormore cysteine residues that are not necessary for function. Variants canbe designed so as to retain or have enhanced biological activity of aparticular region of the protein (e.g., a functional domain, catalyticamino acid residues, etc). Variants also include fragments of thepolypeptides disclosed herein, particularly biologically activefragments and/or fragments corresponding to functional domains.Techniques for in vitro mutagenesis of cloned genes are known. Alsoincluded in the subject invention are polypeptides that have beenmodified using ordinary molecular biological techniques so as to improvetheir resistance to proteolytic degradation or to optimize solubilityproperties or to render them more suitable as a therapeutic agent.

Chimeric antibodies may be made by recombinant means by combining thevariable light and heavy chain regions (V_(L) and V_(H)), obtained fromantibody producing cells of one species with the constant light andheavy chain regions from another. Typically chimeric antibodies utilizerodent or rabbit variable regions and human constant regions, in orderto produce an antibody with predominantly human domains. The productionof such chimeric antibodies is well known in the art, and may beachieved by standard means (as described, e.g., in U.S. Pat. No.5,624,659, incorporated herein by reference in its entirety). It isfurther contemplated that the human constant regions of chimericantibodies of the invention may be selected from IgG1, IgG2, IgG3 orIgG4 constant regions.

Humanized antibodies are engineered to contain even more human-likeimmunoglobulin domains, and incorporate only thecomplementarity-determining regions of the animal-derived antibody. Thisis accomplished by carefully examining the sequence of thehyper-variable loops of the variable regions of the monoclonal antibody,and fitting them to the structure of the human antibody chains. Althoughfacially complex, the process is straightforward in practice. See, e.g.,U.S. Pat. No. 6,187,287, incorporated fully herein by reference. Methodsof humanizing antibodies have been described previously in issued U.S.Pat. No. 7,935,340, the disclosure of which is incorporated herein byreference in its entirety. In some instances, a determination of whetheradditional rabbit framework residues are required to maintain activityis necessary. In some instances the humanized antibodies still requiressome critical rabbit framework residues to be retained to minimize lossof affinity or activity. In these cases, it is necessary to changesingle or multiple framework amino acids from human germline sequencesback to the original rabbit amino acids in order to have desiredactivity. These changes are determined experimentally to identify whichrabbit residues are necessary to preserve affinity and activity.

In addition to entire immunoglobulins (or their recombinantcounterparts), immunoglobulin fragments comprising the epitope bindingsite (e.g., Fab′, F(ab′)₂, or other fragments) may be synthesized.“Fragment,” or minimal immunoglobulins may be designed utilizingrecombinant immunoglobulin techniques. For instance “Fv” immunoglobulinsfor use in the present invention may be produced by synthesizing a fusedvariable light chain region and a variable heavy chain region.Combinations of antibodies are also of interest. e.g. diabodies, whichcomprise two distinct Fv specificities. In another embodiment of theinvention, SMIPs (small molecule immunopharmaceuticals), camelbodies,nanobodies, and IgNAR are encompassed by immunoglobulin fragments.

Immunoglobulins and fragments thereof may be modifiedpost-translationally, e.g. to add effector moieties such as chemicallinkers, detectable moieties, such as fluorescent dyes, enzymes, toxins,substrates, bioluminescent materials, radioactive materials,chemiluminescent moieties and the like, or specific binding moieties,such as streptavidin, avidin, or biotin, and the like may be utilized inthe methods and compositions of the present invention. Examples ofadditional effector molecules are provided infra.

As used herein, “half antibody”. “half-antibody species” or “HIL1” referto a protein complex that includes a single heavy and single lightantibody chain, but lacks a covalent linkage to a second heavy and lightantibody chain. Two half antibodies may remain non-covalently associatedunder some conditions (which may give behavior similar to a fullantibody. e.g., apparent molecular weight determined by size exclusionchromatography). Similarly, H2L1 refers to a protein complex thatincludes two heavy antibody chains and single light antibody chain, butlacks a covalent linkage to a second light antibody chain; thesecomplexes may also non-covalently associate with another light antibodychain (and likewise give similar behavior to a full antibody). Like fullantibodies, half antibody species and H2L1 species can dissociate underreducing conditions into individual heavy and light chains. Halfantibody species and H2L1 species can be detected on a non-reducedSDS-PAGE gel as a species migrating at a lower apparent molecular weightthan the full antibody, e.g., H1L1 migrates at approximately half theapparent molecular weight of the full antibody (e.g., about 75 kDa).

As used herein, “polyploid yeast that stably expresses or expresses adesired secreted heterologous polypeptide for prolonged time” refers toa yeast culture that secretes said polypeptide for at least several daysto a week, more preferably at least a month, still more preferably atleast 1-6 months, and even more preferably for more than a year atthreshold expression levels, typically at least 50-500 mg/liter (afterabout 90 hours in culture) and preferably substantially greater.

As used herein, “polyploidal yeast culture that secretes desired amountsof recombinant polypeptide” refers to cultures that stably or forprolonged periods secrete at least at least 50-500 mg/liter, and mostpreferably 500-1000 mg/liter or more.

A polynucleotide sequence “corresponds” to a polypeptide sequence iftranslation of the polynucleotide sequence in accordance with thegenetic code yields the polypeptide sequence (i.e., the polynucleotidesequence “encodes” the polypeptide sequence), one polynucleotidesequence “corresponds” to another polynucleotide sequence if the twosequences encode the same polypeptide sequence.

A “heterologous” region or domain of a DNA construct is an identifiablesegment of DNA within a larger DNA molecule that is not found inassociation with the larger molecule in nature. Thus, when theheterologous region encodes a mammalian gene, the gene will usually beflanked by DNA that does not flank the mammalian genomic DNA in thegenome of the source organism. Another example of a heterologous regionis a construct where the coding sequence itself is not found in nature(e.g., a cDNA where the genomic coding sequence contains introns, orsynthetic sequences having codons different than the native gene).Allelic variations or naturally-occurring mutational events do not giverise to a heterologous region of DNA as defined herein.

A “coding sequence” is an in-frame sequence of codons that (in view ofthe genetic code) correspond to or encode a protein or peptide sequence.Two coding sequences correspond to each other if the sequences or theircomplementary sequences encode the same amino acid sequences. A codingsequence in association with appropriate regulatory sequences may betranscribed and translated into a polypeptide. A polyadenylation signaland transcription termination sequence will usually be located 3′ to thecoding sequence. A “promoter sequence” is a DNA regulatory regioncapable of binding RNA polymerase in a cell and initiating transcriptionof a downstream (3′ direction) coding sequence. Promoter sequencestypically contain additional sites for binding of regulatory molecules(e.g., transcription factors) which affect the transcription of thecoding sequence. A coding sequence is “under the control” of thepromoter sequence or “operatively linked” to the promoter when RNApolymerase binds the promoter sequence in a cell and transcribes thecoding sequence into mRNA, which is then in turn translated into theprotein encoded by the coding sequence.

Vectors are used to introduce a foreign substance, such as DNA, RNA orprotein, into an organism or host cell. Typical vectors includerecombinant viruses (for polynucleotides) and liposomes (forpolypeptides). A “DNA vector” is a replicon, such as plasmid, phage orcosmid, to which another polynucleotide segment may be attached so as tobring about the replication of the attached segment. An “expressionvector” is a DNA vector which contains regulatory sequences which willdirect polypeptide synthesis by an appropriate host cell. This usuallymeans a promoter to bind RNA polymerase and initiate transcriptionofmRNA, as well as ribosome binding sites and initiation signals todirect translation of the mRNA into a polypeptide(s). Incorporation of apolynucleotide sequence into an expression vector at the proper site andin correct reading frame, followed by transformation of an appropriatehost cell by the vector, enables the production of a polypeptide encodedby said polynucleotide sequence.

“Amplification” of polynucleotide sequences is the in vitro productionof multiple copies of a particular nucleic acid sequence. The amplifiedsequence is usually in the form of DNA. A variety of techniques forcarrying out such amplification are described in the following reviewarticles, each of which is incorporated by reference herein in itsentirety: Van Brunt 1990. Bio/Technol., 8(4):291-294: and Gill andGhaemi, Nucleosides Nucleotides Nucleic Acids. 2008 March; 27(3):224-43.Polymerase chain reaction or PCR is a prototype of nucleic acidamplification, and use of PCR herein should be considered exemplary ofother suitable amplification techniques.

The general structure of antibodies in most vertebrates (includingmammals) is now well understood (Edelman. G. M., Ann. N.Y. Acad. Sci.,190: 5 (1971)). Conventional antibodies consist of two identical lightpolypeptide chains of molecular weight approximately 23,000 daltons (the“light chain”), and two identical heavy chains of molecular weight53,000-70,000 (the “heavy chain”). The four chains are joined bydisulfide bonds in a “Y” configuration wherein the light chains bracketthe heavy chains starting at the mouth of the “Y” configuration. The“branch” portion of the “Y” configuration is designated the F_(b)region; the stem portion of the “Y” configuration is designated theF_(C) region. The amino acid sequence orientation runs from theN-terminal end at the top of the “Y” configuration to the C-terminal endat the bottom of each chain. The N-terminal end possesses the variableregion having specificity for the antigen that elicited it, and isapproximately 100 amino acids in length, there being slight variationsbetween light and heavy chain and from antibody to antibody.

The variable region is linked in each chain to a constant region thatextends the remaining length of the chain and that within a particularclass of antibody does not vary with the specificity of the antibody(i.e., the antigen eliciting it). There are five known major classes ofconstant regions that determine the class of the immunoglobulin molecule(IgG, IgM, IgA, IgD, and IgE corresponding to gamma, mu, alpha, delta,and epsilon heavy chain constant regions). The constant region or classdetermines subsequent effector function of the antibody, includingactivation of complement (Kabat. E. A., Structural Concepts inImmunology and Immunochemistry, 2nd Ed., p. 413-436, Holt, Rinehart,Winston (1976)), and other cellular responses (Andrews, D. W., et al.,Clinical Immunobiology, pp 1-18, W. B. Sanders (1980); Kohl, S., et al.,Immunology, 48: 187 (1983)): while the variable region determines theantigen with which it will react. Light chains are classified as eitherkappa or lambda. Each heavy chain class can be paired with either kappaor lambda light chain. The light and heavy chains are covalently bondedto each other, and the “tail” portions of the two heavy chains arebonded to each other by covalent disulfide linkages when theimmunoglobulins are generated either by hybridomas or by B cells.

The expression “variable region” or “VR” refers to the domains withineach pair of light and heavy chains in an antibody that are involveddirectly in binding the antibody to the antigen. Each heavy chain has atone end a variable domain (V_(L)) followed by a number of constantdomains. Each light chain has a variable domain (V_(L)) at one end and aconstant domain at its other end; the constant domain of the light chainis aligned with the first constant domain of the heavy chain, and thelight chain variable domain is aligned with the variable domain of theheavy chain.

The expressions “complementarity determining region,” “hypervariableregion,” or “CDR” refer to one or more of the hyper-variable orcomplementarity determining regions (CDRs) found in the variable regionsof light or heavy chains of an antibody (See Kabat, E. A. et al.,Sequences of Proteins of Immunological Interest, National Institutes ofHealth, Bethesda, Md., (1987)). These expressions include thehypervariable regions as defined by Kabat et al. (“Sequences of Proteinsof Immunological Interest,” Kabat E., et al., US Dept. of Health andHuman Services, 1983) or the hypervariable loops in 3-dimensionalstructures of antibodies (Chothia and Lesk, J Mol. Biol. 196 901-917(1987)). The CDRs in each chain are held in close proximity by frameworkregions and, with the CDRs from the other chain, contribute to theformation of the antigen binding site. Within the CDRs there are selectamino acids that have been described as the selectivity determiningregions (SDRs) which represent the critical contact residues used by theCDR in the antibody-antigen interaction (Kashmiri. S., Methods. 36:25-34(2005)).

The expressions “framework region” or “FR” refer to one or more of theframework regions within the variable regions of the light and heavychains of an antibody (See Kabat, E. A. et al., Sequences of Proteins ofImmunological Interest, National Institutes of Health, Bethesda, Md.,(1987)). These expressions include those amino acid sequence regionsinterposed between the CDRs within the variable regions of the light andheavy chains of an antibody.

The expression “stable copy number” refers to a host cell thatsubstantially maintains the number of copies of a gene (such as anantibody chain gene) over a prolonged period of time (such as at least aday, at least a week, or at least a month, or more) or over a prolongednumber of generations of propagation (e.g., at least 30, 40, 50, 75,100, 200, 500, or 1000 generations, or more). For example, at a giventime point or number of generations, at least 50%, and preferably atleast 70%. 75%, 85%, 90%, 95%, or more of cells in the culture maymaintain the same number of copies of the gene as in the starting cell.In a preferred embodiment, the host cell contains a stable copy numberof the gene encoding the desired protein or encoding each subunit of thedesired multi-subunit complex (e.g., antibody).

The expression “stably expresses” refers to a host cell that maintainssimilar levels of expression of a gene or protein (such as an antibody)over a prolonged period of time (such as at least a day, at least aweek, or at least a month, or more) or over a prolonged number ofgenerations of propagation (e.g., at least 30, 40, 50, 75, 100, 200,500, or 1000 generations, or more). For example, at a given time pointor number of generations, the rate of production or yield of the gene orprotein may be at least 50%, and preferably at least 70%, 75%, 85%, 90%,95%, or more of the initial rate of production. In a preferredembodiment, the host cell stably expresses the desired protein ormulti-subunit complex (e.g., antibody).

Recovery and Purification of Recombinant Proteins

Monoclonal antibodies have become prominent therapeutic agents, buttheir purification process needs to reliably and predictably produce aproduct suitable for use in humans. Impurities such as host cellprotein, DNA, adventitious and endogenous viruses, endotoxin, aggregatesand other species. e.g., glycovariants, must be controlled whilemaintaining an acceptable yield of the desired antibody product. Inaddition, impurities introduced during the purification process (e.g.,leached Protein A, extractables from resins and filters, process buffersand agents such as detergents) must be removed as well before theantibody can be used as a therapeutic agent.

Primary Recovery Processes

The first step in the recovery of an antibody from cell culture isharvest. Cells and cell debris are removed to yield a clarified,filtered fluid suitable for chromatography. i.e., harvested cell culturefluid (HCCF). Exemplary methods for primary recovery includecentrifugation, depth filtration and sterile filtration, flocculation,precipitation and/or other applicable approaches depending on scale andfacility capability.

Centrifugation

In one embodiment, cells and flocculated debris are removed from brothby centrifugation. Centrifugation can be used for pilot and commercialscale manufacturing. Preferably, centrifugation is used in large scalemanufacturing to provide harvested cell culture fluid from cell cultureswith percent solids of >3% (i.e., increased levels of sub-microndebris).

Standard non-hermetic disc-stack centrifuges as well fully hermeticcentrifuges as are capable of removing cells and large cell debris,although fully hermetic centrifuges can significantly reduce the amountof cell lysis that is incurred during this unit operation, e.g., by atleast 50%, by preventing overflow and minimizing shear.

The clarification efficiency of the centrifugation process is affectedby harvest parameters such as centrifuge feed rate. G-force, bowlgeometry, operating pressures, discharge frequency and ancillaryequipment used in the transfer of cell culture fluid to the centrifuge.The cell culture process characteristics such as peak cell density,total cell density and culture viability during the culture process andat harvest can also affect separation performance. The centrifugationprocess can be optimized to select the feed rate and bowl rotationalspeed using the scaling factors of feed rate (Q) and equivalent settlingarea (Σ) in the centrifuge. The optimized process can minimize celllysis and debris generation while maximizing the sedimentation ofsubmicron particles and product yield.

Filtration

Tangential flow microfiltration can also be used in cell harvest. Inparticular, the cell culture fluid flows tangential to the microporousmembrane, and pressure driven filtrate flow separates the solubleproduct from the larger, insoluble cells. Membrane fouling is limited bythe inertial lift and shear-induced diffusion generated by the turbulentflow across the membrane surface.

A high yielding harvest can be achieved by a series of concentration anddiafiltration steps. In the former, the volume of the cell culture fluidis reduced, which results in concentrating the solid mass. Thediafiltration step then washes the product from the concentrated cellculture fluid mixture.

By way of example, a 0.22 μm pore size may be employed for the TFFmembrane as it produces the target quality harvested cell culture fluid(suitable for chromatography) without the need for furtherclarification. Alternatively, more open pore sizes at the TFF barriermay be used to better manage fouling; however, more open pore sizes mayrequire an additional clarification step (e.g., normal flow depthfiltration) downstream of the TFF system. Preferably, TFF is used forcell cultures with percent solids of <3%.

Depth filters can also be used in the clarification of cell culturebroths, to maintain capacity on membrane filters or to protectchromatography columns or virus filters. Depth filters may be composedof, e.g., cellulose, a porous filter-aid such as diatomaceous earth, anionic charged resin binder and a binding resin (present at a smallweight percent to covalently bind dissimilar construction materialstogether, giving the resultant media wet strength and conferringpositive charge to the media surfaces). Depth filters rely on both sizeexclusion and adsorptive binding to effect separation. Exemplary depthfilters are approximately 2-4 mm thick.

For harvesting applications, depth filters can be applied directly withthe whole cell broth or in conjunction with a primary separator, e.g.,TFF or centrifugation. For example, when used for whole-cell broth depthfilter harvest, the filtration train contains three stages of filters:(1) the primary stage with a coarse or open depth filter with a poresize of up to 10 μm to remove whole cells and large particles; (2) thesecondary stage with a tighter depth filter to clear colloidal andsubmicron particles; and (3) the third stage with a 0.2 μm pore sizemembrane filter. Although the filtration process generally scaleslinearly, a safety factor of 1.5× to >3× can be employed for each stageto ensure adequate filter capacity.

In one embodiment, a depth filter is employed after centrifugation tofurther clarify the harvested broth, e.g., because there is a practicallower limit to the particle size that can be removed by centrifugation.For example, the depth filter may comprise two distinct layers (with theupstream zone being a coarser grade compared with the downstream) andhave a pore size range of 0.1-4 μm. The larger particles are trapped inthe coarse grade filter media and smaller particles are trapped in thetighter media, reducing premature plugging and increasing filtrationcapacity.

Optimization of filter type, pore size, surface area and flux can bedone at lab bench scale and then scaled up to pilot scale based on,e.g., the centrate turbidity and particle size distribution. Depthfilter sizing experiments are generally performed at constant flux usingpressure endpoints in any one or combination of filtration stages.Preferably, a 0.22 μm grade filter is used to filter the supernatant atthe end of harvest process to control bioburden. The 0.22 μm-filteredsupernatant can be stored at 2-8° C. for several days or longer withoutchanging the antibody product-related variant profile.

Without being bound by theory, it is believed that the adsorptivemechanism of depth filters allows for their extensive use as apurification tool to remove a wide range of process contaminants andimpurities. In particular, the electrostatic interactions between thepositive charges of depth filters and DNA molecules as well ashydrophobic interactions between depth filter media and DNA moleculesmay play important roles in the adsorptive reduction of DNA. Forexample, charged depth filters have been used to remove DNA, and thelevel of charges on Zeta Plus (Cuno) 90SP has been correlated with itsability to remove DNA. Additionally, by way of example, positivelycharged depth filters have been used to remove Escherichia coli-derivedand other endogenous endotoxins and viruses many times smaller than theaverage pore size of the filter, and Zeta Plus® (Cuno) VR series depthfilters were found to bind enveloped retrovirus and non-envelopedparvovirus by adsorption. Depth filtration was also employed to removespiked prions from an immunoglobin solution. Moreover, the removal ofhost cell proteins through depth filtration prior to a Protein Aaffinity chromatography column has been shown to significantly reduceprecipitation during the pH adjustment of the Protein A pool.

Flocculation and Precipitation

In one embodiment, precipitation/flocculation-based pretreatment stepsare used to reduce the quantity of cell debris and colloids in the cellculture fluid, which can exceed the existing filtration train equipmentcapability. Flocculation involves polymer adsorption, e.g.,electrostatic attraction, to the cell and cell debris by, e.g.,cationic, neutral and anionic polymers, to clear cellular contaminantsresulting in improved clarification efficiency and high recovery yield.Flocculation reagents. e.g., calcium chloride and potassium phosphate,at very low levels. e.g., 20-60 mM calcium chloride with an equimolaramount of phosphate added to form calcium phosphate, are believed tocontribute to co-precipitation of calcium phosphate with cells, celldebris and impurities.

In one embodiment, the disclosed purification processes includetreatment of the whole cell broth with ethylene diamine tetraacetic acid(EDTA) to 3 mM final concentration and with a flocculating agent,subsequent removal of cells and flocculated debris by centrifugation,followed by clarification through depth and 0.2 μm filters.

Chromatography

In the biopharmaceutical industry, chromatography is a critical andwidely used separation and purification technology due to its highresolution. Chromatography exploits the physical and chemicaldifferences between biomolecules for separation. For example, protein Achromatography may follow harvest to yield a relatively pure productthat requires removal of only a small proportion of process and productrelated impurities. One or two additional chromatography steps can thenbe employed as polishing steps, e.g., incorporating ion exchangechromatography, hydrophobic interaction chromatography, mixed modechromatography and/or hydroxyapatite chromatography. These steps canprovide additional viral, host cell protein and DNA clearance, as wellas removing aggregates, unwanted product variant species and other minorcontaminants. Lastly, the purified product may be concentrated anddiafiltered into the final formulation buffer.

Antibody purification involves selective enrichment or specificisolation of antibodies from serum (polyclonal antibodies), ascitesfluid or cell culture supernatant of a cell line (monoclonalantibodies). Purification methods range from very crude to highlyspecific and can be classified as follows:

Physicochemical fractionation—differential precipitation, size-exclusionor solid-phase binding of immunoglobulins based on size, charge or othershared chemical characteristics of antibodies in typical samples. Thisisolates a subset of sample proteins that includes the immunoglobulins.

Affinity fractionation—binding of particular antibody classes (e.g.,IgG) by immobilized biological ligands (e.g., proteins) that havespecific affinity to immunoglobulins (which purifies all antibodies ofthe target class without regard to antigen specificity) or affinitypurification of only those antibodies in a sample that bind to aparticular antigen molecule through their specific antigen-bindingdomains (which purifies all antibodies that bind the antigen withoutregard to antibody class or isotype).

The main classes of serum immunoglobulins (e.g., IgG and IgM) share thesame general structure, including overall amino acid composition andsolubility characteristics. These general properties are sufficientlydifferent from most other abundant proteins in serum, e.g., albumin andtransferrin, that the immunoglobulins can be selected and enriched foron the basis of these differentiating physicochemical properties.

Physiochemical Fractionation Antibody Purification

Ammonium Sulfate Precipitation

Ammonium sulfate precipitation is frequently used to enrich andconcentrate antibodies from serum, ascites fluid or cell culturesupernatant. As the concentration of the lyotropic salt is increased ina sample, proteins and other macromolecules become progressively lesssoluble until they precipitate, i.e., the lyotropic effect is referredto as “salting out.” Antibodies precipitate at lower concentrations ofammonium sulfate than most other proteins and components of serum.

At about 40 to about 50% ammonium sulfate saturation (100% saturationbeing equal to 4.32M), immunoglobulins precipitate while other proteinsremain in solution. See, e.g., Harlow, E. and Lane, D. (1988).Antibodies: A Laboratory Manual. Cold Spring Harbor Laboratory Press,Cold Spring Harbor, N.Y. Gagnon, P. (1996). By way of example, an equalvolume of saturated ammonium sulfate solution is slowly added to aneutralized antibody sample, followed by incubation for several hours atroom temperature or 4° C. After centrifugation and removal of thesupernatant, the antibody-pellet is dissolved in buffer, such asphosphate-buffered saline (PBS).

The selectivity, yield, purity and reproducibility of precipitationdepends upon several factors including, but not limited to, time,temperature, pH and rate of salt addition. See, e.g., Gagnon, P. S.(1996). Purification Tools for Monoclonal Antibodies. ValidatedBiosystems. Tucson, Ariz. Ammonium sulfate precipitation may providesufficient purification for some antibody applications, but often it isperformed as a preliminary step before column chromatography or otherpurification method. Using partially-purified antibody samples canimprove the performance and extend the life of affinity columns.

Suitable antibody precipitation reagents other than ammonium sulfate forantibody purification situations include, by way of example, octonoicacid, polyethylene glycol and ethacridine.

Numerous chemically-based, solid-phase chromatography methods have beenadapted and optimized to achieve antibody purification in particularsituations.

Ion Exchange Chromatography (IEC)

Ion exchange chromatography (IEC) uses positively or negatively chargedresins to bind proteins based on their net charges in a given buffersystem (pH). Conditions for IEC can be determined that bind and releasethe target antibody with a high degree of specificity, which may beespecially important in commercial operations involving production ofmonoclonal antibodies. Conversely, conditions can be found that bindnearly all other sample components except antibodies. Once optimized,IEC is a cost-effective, gentle and reliable method for antibodypurification.

Anion exchange chromatography uses a positively charged groupimmobilized to the resin. For example, weakly basic groups such asdiethylamino ethyl (DEAE) or dimethylamino ethyl (DMAE), or stronglybasic groups such as quaternary amino ethyl (Q) or trimethylammoniumethyl (TMAE) or quaternary aminoethyl (QAE)) can be used in anionexchange. Exemplary anion exchange media include, but are not limitedto, GE Healthcare Q-Sepharose FF, Q-Sepharose BB, Q-Sepharose XL,Q-Sepharose HP, Mini Q. Mono Q, Mono P. DEAE Sepharose FF, Source 15Q,Source 30Q, Capto Q. Streamline DEAE, Streamline QXL; Applied BiosystemsPoros HQ 10 and 20 um self pack, Poros HQ 20 and 50 um, Poros PI 20 and50 um, Poros D 50 um; Tosohaas Toyopearl DEAE 650S M and C. Super Q 650,QAE 550C; Pall Corporation DEAE Hyper D, Q Ceramic Hyper D, Mustang Qmembrane absorber: Merck KG2A Fractogel DMAE, FractoPrep DEAE,Fractoprep TMAE. Fractogel EMD DEAE, Fractogel EMD TMAE; SartoriousSartobind Q membrane absorber.

Anion exchange is particularly useful for removing process-relatedimpurities (e.g., host cell proteins, endogenous retrovirus andadventitious viruses such as parvovirus or pseudorabies virus. DNA,endotoxin and leached Protein A) as well as product-related impurities(e.g., dimer/aggregate). It can be used either in flow-through mode orin bind and elute mode, depending on the pI of the antibody andimpurities to be removed. For example, flow-through mode is preferablyused to remove impurities from antibodies having a pI above 7.5, e.g.,most humanized or human IgG1 and IgG2 antibodies, because the impuritiesbind to the resin and the product of interest flows through. The columnloading capacity, i.e., mass of antibody to mass of resin, can be quitehigh since the binding sites on the resin are occupied only by theimpurities. Anion exchange chromatography in flow-through mode may beused as a polishing step in monoclonal antibody purification processesdesigned with two or three unit operations to remove residual impuritiessuch as host cell protein, DNA, leached Protein A and a variety ofviruses. By way of example, the operating pH is about 8 to about 8.2,with a conductivity of up to 10 mS/cm in the product load andequilibration and wash buffers.

Alternatively, bind and elute mode is preferably used to removeprocess-related and product-related impurities from antibodies having apI in the acidic to neutral range, e.g., most humanized or human IgG4s.For bind-and-elute mode, the antibody product pool is first loaded ontoan anion exchange column and the product of interest is then eluted witha higher salt concentration in a step or linear gradient, leaving themajority of impurities bound to the column. The impurities are elutedfrom the column during the cleaning or regeneration step. Generally, theoperating pH should be above or close to the pI of the product in orderto obtain a net negative charge or higher negative charge number on thesurface of the antibody molecules, and, thus, to achieve a higherbinding capacity during the chromatography step. Similarly, the ionicstrength for the load is preferably in the low range and the pH ispreferably less than pH 9.

Additionally, weak partitioning chromatography (WPC) may be used toenable a two chromatography recovery process comprising Protein A andanion exchange. Generally, the process is run isocratically (as withflow-through chromatography) but the conductivity and pH are chosen suchthat the binding of both the product and impurities are enhanced (incontrast to flow-through mode), attaining an antibody partitioncoefficient (Kp) between 0.1-20, and preferably between 1 and 3. Bothantibody and impurities bind to the anion exchange resin, but theimpurities are much more tightly bound than in flow-through mode, whichcan lead to an increase in impurity removal. Product yield in weakpartitioning mode can be maximized by including a short wash at the endof the load, e.g., averaged 90% for clinical production.

Cation exchange chromatography uses a resin modified with negativelycharged functional groups. For example, strong acidic ligands (e.g.,sulfopropyl, sulfoethyl and sulfoisobutyl groups) or weak acidic ligands(e.g., carboxyl group) can be used in cation exchange. Exemplary cationexchange resins include, but are not limited to, GE HelalthcareSP-Sepharose FF. SP-Sepharose BB. SP-Sepharose XL, SP-Sepharose HP. MiniS. Mono S, CM Sepharose FF, Source 15S, Source 30S. Capto S, MacroCapSP. Streamline SP-XL. Streamline CST-1: Tosohaas Resins Toyopearl MegaCap TI SP-550 EC, Toyopearl Giga Cap S-650M. Toyopearl 650S, M and C,Toyopeal SP650S, M. and C, Toyopeal SPS50C: TF Baker ResinsCarboxy-Sulphon-5, 15 and 40 um. Sulfonic-5, 15, and 40 um; YMC BioProS; Applied Biosystems Poros HS 20 and 50 um. Poros S 10 and 20 um; PallCorp S Ceramic Hyper D, CM Ceramic Hyper D; Merck KGgA Resins FractogelEMD SO₃, Fractogel EMD COO-, Fractogel EMD SE Hicap, Fracto Prep SO3:Eshmuno S; Biorad Resin Unosphere S; Sartorius Membrane Sartobind Smembrane absorber.

Cation exchange chromatography is particularly suited for purificationprocesses for many monoclonal antibodies with pI values ranging fromneutral to basic, e.g., human or humanized IgG1 and IgG2 subclasses. Ingeneral, the antibody is bound onto the resin during the loading stepand eluted through either increasing conductivity or increasing pH inthe elution buffer. The most negatively charged process-relatedimpurities such as DNA, some host cell protein, leached Protein A andendotoxin are removed in the load and wash fraction. Cation exchangechromatography can also reduce antibody variants from the targetantibody product such as deamidated products, oxidized species andN-terminal truncated forms, as well as high molecular weight species.

The maximum binding capacity attained can be as high as >100 g/L ofresin volume depending on the loading conditions, resin ligand anddensity, but impurity removal depends highly on the loading density. Thesame principles described for anion exchange chromatography regardingdevelopment of the elution program apply to cation exchangechromatography as well.

The development of elution conditions is linked to impurity removal andcharacteristics of the product pool that can be processed easily in thesubsequent unit operation. Generally, a linear salt or pH gradientelution program can be conducted to determine the best elutioncondition. For example, linear gradient elution conditions may rangefrom 5 mM to 250 mM NaCl at pH 6 and linear pH gradient elution runs mayrange from pH 6 to pH 8.

Immobilized Metal Chelate Chromatography (IMAC)

Immobilized metal chelate chromatography (IMAC) uses chelate-immobilizeddivalent metal ions (e.g., nickel Ni2+) to bind proteins or peptidesthat contain clusters of three or more consecutive histidine residues.This strategy can be particularly useful for purification of recombinantproteins that have been engineered to contain a terminal 6×His fusiontag. Mammalian IgGs are one of the few abundant proteins in serum (ormonoclonal cell culture supernatant) that possess histidine clusterscapable of being bound by immobilized nickel. Like IEC, IMAC conditionsfor binding and elution can be optimized for particular samples toprovide gentle and reliable antibody purification. For example, IMAC maybe used to separate AP- or HRP-labeled (enzyme-conjugated) antibody fromexcess, non-conjugated enzyme following a labeling procedure.

Hydrophobic Interaction Chromatography (HIC)

Hydrophobic interaction chromatography (HIC) separates proteins based ontheir hydrophobicity, and is complementary to other techniques thatseparate proteins based on charge, size or affinity. For example, asample loaded on the HIC column in a high salt buffer which reducessolvation of the protein molecules in solution, thereby exposinghydrophobic regions in the sample protein molecules that consequentlybind to the HIC resin. Generally, the more hydrophobic the molecule, theless salt is needed to promote binding. A gradient of decreasing saltconcentration can then be used to elute samples from the HIC column. Inparticular, as the ionic strength decreases, the exposure of thehydrophilic regions of the molecules increases and molecules elute fromthe column in order of increasing hydrophobicity.

HIC in flow-through mode can be efficient in removing a large percentageof aggregates with a relatively high yield. HIC in bind-and-elute modemay provides effective separation of process-related and product-relatedimpurities from antibody product. In particular, the majority of hostcell protein, DNA and aggregates can be removed from the antibodyproduct through selection of a suitable salt concentration in theelution buffer or use of a gradient elution method.

Exemplary HIC resins include, but are not limited to, GE Healthcare HICResins (Butyl Sepharose 4 FF, Butyl-S Sepharose FF, Octyl Sepharose 4FF. Phenyl Sepharose BB. Phenyl Sepharose HP, Phenyl Sepharose 6 FF HighSub, Phenyl Sepharose 6 FF Low Sub, Source 15ETH, Source 15ISO, Source15PHE, Capto Phenyl, Capto Butyl, Sreamline Phenyl); Tosohaas HIC Resins(TSK Ether 5PW (20 um and 30 um), TSK Phenyl 5PW (20 um and 30 um),Phenyl 650S, M, and C, Butyl 650S. M and C, Hexyl-650M and C, Ether-650Sand M, Butyl-600M. Super Butyl-550C, Phenyl-600M; PPG-600M); Waters HICResins (YMC-Pack Octyl Columns-3, 5, 10P, 15 and 25 um with pore sizes120, 200, 300 A, YMC-Pack Phenyl Columns-3, 5, 10P, 15 and 25 um withpore sizes 120, 200 and 300 A. YMC-Pack Butyl Columns-3, 5, 10P, 15 and25 um with pore sizes 120, 200 and 300 A); CHISSO Corporation HIC Resins(Cellufine Butyl. Cellufine Octyl, Cellufine Phenyl); JT Baker HIC Resin(WP HI-Propyl (C3)); Biorad HIC Resins (Macroprep t-Butyl, Macroprepmethyl); and Applied Biosystems HIC Resin (High Density Phenyl-HP2 20um). For example, PPG 600-M is characterized by an exclusion limitmolecular weight of approximately 8×10⁵ Dalton, a polypropylene glycolPPG ligand, a 45-90 μm particle size, hydrophobicity given by therelationship Ether>PPG>Phenyl, and Dynamic Binding capacity (MAb: AntiLH) of 38 mg/mL-gel.

In one embodiment, the disclosed purification processes employhydrophobic interaction chromatography (HIC) as a polish purificationstep after affinity chromatography (e.g., Protein A) and mixed modechromatography (e.g., hydroxyapatite). See, FIG. 1. Preferably,polypropylene glycol (PPG-600M) or Phenyl-600M is the HIC resin. In oneembodiment, the elution is performed as a linear gradient (0-100%) fromabout 0.7 M to 0 M sodium sulfate in a 20 mM sodium phosphate, pH 7,buffer. Optionally the OD₂₈₀ of the effluent is monitored and a seriesof fractions, e.g., about one-third of the collection volume, iscollected for further purity analysis. Preferably, the fractionscollected include from 0.1 OD on the front flank to 0.1 OD on the rearflank.

Hydrophobic Charge Induction Chromatography (HCIC)

Hydrophobic charge induction chromatography (HCIC) is based on thepH-dependent behavior of ligands that ionize at low plH. This techniqueemploys heterocyclic ligands at high densities so that adsorption canoccur via hydrophobic interactions without the need for highconcentrations of lyotropic salts. Desorption in HCIC is facilitated bylowering the pH to produce charge repulsion between the ionizable ligandand the bound protein. An exemplary commercial HCIC resin isMEP-Hypercel (Pall Corporation), which is a cellulose-based media with4-mercaptoethyl pyridine as the functional group. The ligand is ahydrophobic moiety with an N-heterocyclic ring that acquires a positivecharge at low pH.

Thiophilic Adsorption

Thiophilic adsorption is a highly selective type of protein-ligandinteraction, combining the properties of hydrophobic interactionchromatography (IHIC) and ammonium sulfate precipitation (i.e., thelyotropic effect), that involves the binding of proteins to a sulfonegroup in close proximity to a thioether. In contrast to strict HIC,thiophilic adsorption depends upon a high concentration of lyotropicsalt (e.g., potassium sulfate as opposed to sodium chloride). Forexample, binding is quite specific for a typical antibody sample thathas been equilibrated with potassium sulfate. After non-bound componentsare washed away, the antibodies are easily recovered with gentle elutionconditions (e.g., 50 mM sodium phosphate buffer, pH 7 to 8). ThiophilicAdsorbent (also called T-Gel) is 6% beaded agarose modified to containthe sulfone-thiocther ligand, which has a high binding capacity andbroad specificity toward immunoglobulin from various animal species.

Affinity Purification of Antibodies

Affinity chromatography (also called affinity purification) makes use ofspecific binding interactions between molecules. Generally, a particularligand is chemically immobilized or “coupled” to a solid support so thatwhen a complex mixture is passed over the column, those molecules havingspecific binding affinity to the ligand become bound. After other samplecomponents are washed away, the bound molecule is stripped from thesupport, resulting in its purification from the original sample.

Supports

Affinity purification involves the separation of molecules in solution(mobile phase) based on differences in binding interaction with a ligandthat is immobilized to a stationary material (solid phase). A support ormatrix in affinity purification is any material to which a biospecificligand is covalently attached. Typically, the material to be used as anaffinity matrix is insoluble in the system in which the target moleculeis found. Usually, but not always, the insoluble matrix is a solid.

Useful affinity supports are those with a high surface-area to volumeratio, chemical groups that are easily modified for covalent attachmentof ligands, minimal nonspecific binding properties, good flowcharacteristics and mechanical and chemical stability.

Immobilized ligands or activated affinity support chemistries areavailable for use in several different formats, including, e.g.,cross-linked beaded agarose or polyacrylamide resins and polystyrenemicroplates.

Porous gel supports provide a loose matrix in which sample molecules canfreely flow past a high surface area of immobilized ligand, which isalso useful for affinity purification of proteins. These types ofsupports are usually sugar- or acrylamide-based polymer resins that areproduced in solution (i.e., hydrated) as 50-150 μm diameter beads. Thebeaded format allows these resins to be supplied as wet slurries thatcan be easily dispensed to fill and “pack” columns with resin beds ofany size. The beads are extremely porous and large enough thatbiomolecules (proteins, etc.) can flow as freely into and through thebeads as they can between and around the surface of the beads. Ligandsare covalently attached to the bead polymer (external and internalsurfaces) by various means.

For example, cross-linked beaded agarose is typically available in 4%and 6% densities (i.e., a 1 ml resin-bed is more than 90% water byvolume.) Beaded agarose may be suitable for gravity-flow,low-speed-centrifugation, and low-pressure procedures. Alternatively,polyacrylamide-based, beaded resins generally do not compress and may beused in medium pressure applications with a peristaltic pump or otherliquid chromatography systems. Both types of porous support havegenerally low non-specific binding characteristics. A summary of thephysical properties of these affinity chromatography resins is providedin Table 1 below.

TABLE 1 Physical properties of affinity chromatography resins Physicalproperties of affinity chromatography resins 4% crosslinked 6%crosslinked Acrylamide- Support beaded agarose beaded agarose azlactonepolymer Bead size 45-165 μm 45-165 μm 50-80 μm Exclusion 20,000 kDa4,000 kDa 2,000 kDa limit Durability crushes under crushes under sturdy(>100 psi, high pressure high pressure 6.9 bar) Methods gravity-flow orgravity-flow or FPLC Systems, low-speed low-speed HPLC, gravitycentrifugation centrifugation flow Coupling medium Medium high CapacitypH range 3-11 3-11 1-13 Form pre-swollen pre-swollen dry or pre-swollen

Magnetic particles are yet another type of solid affinity support. Theyare much smaller (typically 1-4 μm diameter), which provides thesufficient surface area-to-volume ratio needed for effective ligandimmobilization and affinity purification. Affinity purification withmagnetic particles is performed in-batch, e.g., a few microliters ofbeads is mixed with several hundred microliters of sample as a looseslurry. During mixing, the beads remain suspended in the samplesolution, allowing affinity interactions to occur with the immobilizedligand. After sufficient time for binding has been given, the beads arecollected and separated from the sample using a powerful magnet.Typically, simple bench-top procedures are done in microcentrifugetubes, and pipetting or decanting is used to remove the sample (or washsolutions, etc.) while the magnetic beads are held in place at thebottom or side of the tube with a suitable magnet.

Magnetic particles are particularly well suited for high-throughputautomation and, unlike porous resins, can be used in lieu of cellseparation procedures.

Each specific affinity system requires its own set of conditions andpresents its own peculiar challenges for a given research purpose.However, affinity purification generally involves the following steps:

1. Incubate crude sample with the affinity support to allow the targetmolecule in the sample to bind to the immobilized ligand;

2. Wash away non-bound sample components from the support; and

3. Elute (dissociate and recover) the target molecule from theimmobilized ligand by altering the buffer conditions so that the bindinginteraction no longer occurs.

Ligands that bind to general classes of proteins (e.g., antibodies) orcommonly used fusion protein tags (e.g., 6×His) are commerciallyavailable in pre-immobilized formnns ready to use for affinitypurification. Alternatively, more specialized ligands such as specificantibodies or antigens of interest can be immobilized using one ofseveral commercially available activated affinity supports; for example,a peptide antigen can be immobilized to a support and used to purifyantibodies that recognize the peptide.

Most commonly, ligands are immobilized or “coupled” directly to solidsupport material by formation of covalent chemical bonds betweenparticular functional groups on the ligand (e.g., primary amines,sulfhydryls, carboxylic acids, aldehydes) and reactive groups on thesupport (see related article on Covalent Immobilization). However,indirect coupling approaches are also possible. For example, aGST-tagged fusion protein can be first captured to a glutathione supportvia the glutathione-GST affinity interaction and then secondarilychemically crosslinked to immobilize it. The immobilized GST-taggedfusion protein can then be used to affinity purify binding partner(s) ofthe fusion protein.

Binding and Elution Buffers for Affinity Purification

Most affinity purification procedures involving protein:ligandinteractions use binding buffers at physiologic pH and ionic strength,such as phosphate buffered saline (PBS), particularly when theantibody:antigen or native protein:protein interactions are the basisfor the affinity purification. Once the binding interaction occurs, thesupport is washed with additional butTer to remove non-bound componentsof the sample. Non-specific (e.g., simple ionic) binding interactionscan be minimized by adding low levels of detergent or by moderateadjustments to salt concentration in the binding and/or wash buffer.Finally, clution buffer (e.g., 0.1 M glycine⋅HCl, pH 2.5-3.0) is addedto break the binding interaction (without permanently affecting theprotein structure) and release the target molecule, which is thencollected in its purified form. Elution buffer can dissociate bindingpartners by extremes of pH (low or high), high salt (ionic strength),the use of detergents or chaotropic agents that denature one or both ofthe molecules, removal of a binding factor or competition with a counterligand. In some cases, subsequent dialysis or desalting may be requiredto exchange the purified protein from elution buffer into a moresuitable buffer for storage or downstream processing.

Additionally, some antibodies and proteins are damaged by low pH, soeluted protein fractions should be neutralized immediately by additionof 1/10th volume of alkaline buffer, e.g., 1 M Tris⋅HCl, pH 8.5. Otherexemplary elution buffers for affinity purification of proteins areprovided in Table 2 below.

TABLE 2 Exemplary elution buffer systems for protein affinitypurification Exemplary elution buffer systems for protein affinitypurification Condition Buffer pH 100 mM glycine•HCl, pH 2.5-3.0 100 mMcitric acid, pH 3.0 50-100 mM triethylamine or triethanolamine, pH 11.5150 mM ammonium hydroxide, pH 10.5 1M arginine, pH 4.0 Ionic strength3.5-4.0 M magnesium chloride, pH 7.0 in 10 mM Tris and/or 5M lithiumchloride in 10 mM phosphate buffer, pH 7.2 chaotrophic 2.5M sodiumiodide, pH 7.5 effects 0.2-3.0 sodium thiocyanate Denaturing 2-6Mguanidinc•HCl 2-8M urea 1% deoxycholate 1% SDS Organic 10% dioxaneCompetitor 50% ethylene glycol, pH 8-11.5 (also chaotropic) >0.1Mcounter ligand or analog

Several methods of antibody purification involve affinity purificationtechniques. Exemplary approaches to affinity purification includeprecipitation with ammonium sulfate (crude purification of totalimmunoglobulin from other serum proteins); affinity purification withimmobilized Protein A. G, A/G or L (bind to most species and subclassesof IgG) or recombinant Protein A, G. A/G, or L, derivatives in bind &elute mode; and affinity purification with immobilized antigen(covalently immobilized purified antigen to an affinity support toisolate specific antibody from crude samples) in bind & elute mode.

Protein A, Protein G and Protein L are three bacterial proteins whoseantibody-binding properties have been well characterized. These proteinshave been produced recombinantly and used routinely for affinitypurification of key antiboxxly types from a variety of species. Mostcommercially-available, recombinant forms of these proteins haveunnecessary sequences removed (e.g., the HSA-binding domain from ProteinG) and are therefore smaller than their native counterparts. Agenetically-engineered recombinant form of Protein A and Protein G,called Protein A/G, is also available. All four recombinant Ig-bindingproteins are used routinely by researchers in numerous immunodetectionand immunoaffinity applications.

To accomplish antibody purification, with Protein A. Protein G. ProteinA/G are covalently immobilized onto a support, e.g., porous resins (suchas beaded agarose) or magnetic beads. Because these proteins containseveral antibody-binding domains, nearly every individual immobilizedmolecule, no matter its orientation maintains at least one functionaland unhindered binding domain. Furthermore, because the proteins bind toantibodies at sites other than the antigen-binding domain, theimmobilized forms of these proteins can be used in purification schemes,such as immunoprecipitation, in which antibody binding protein is usedto purify an antigen from a sample by binding an antibody while it isbound to its antigen.

The high affinity of Protein A for the Fc region of IgG-type antibodiesis the basis for the purification of IgG, IgG fragments and subclasses.Generally, Protein A chromatography involves passage of clarified cellculture supernatant over the column at pH about 6.0 to about 8.0, suchthat the antibodies bind and unwanted components, e.g., host cellproteins, cell culture media components and putative viruses, flowthrough the column. An optional intermediate wash step may be carriedout to remove non-specifically bound impurities from the column,followed by elution of the product at pH about 2.5 to about pH 4.0. Theelution step may be performed as a linear gradient or a step method or acombination of gradient and step. In one embodiment, the eluate isimmediately neutralized with a neutralization buffer (e.g. 1 M Tris, pH8), and then adjusted to a final pH 6.5 using, e.g., 5% hydrochloricacid or 1 M sodium hydroxide. Preferably, the neutralized eluate isfiltered prior to subsequent chromatography. In one embodiment, theneutralized eluate is passed through a 0.2 μm filter prior to thesubsequent hydroxyapatite chromatography step.

Because of its high selectivity, high flow rate and cost effectivebinding capacity and its capacity for extensive removal ofprocess-related impurities such as host cell proteins, DNA, cell culturemedia components and endogenous and adventitious virus particles.Protein A chromatography is typically used as the first step in anantibody purification process. After this step, the antibody product ishighly pure and more stable due to the elimination of proteases andother media components that may cause degradation.

There are currently three major types of Protein A resins, classifiedbased on their resin backbone composition: glass or silica-based, e.g.,AbSolute HiCap (NovaSep). Prosep vA, Prosep vA Ultra (Millipore);agarose-based, e.g., Protein A Sepharose Fast Flow, MabSelect andMabSelect SuRe (GE Healthcare); and organic polymer based. e.g.,polystyrene-divinylbenzene Poros A and MabCapture (Applied Biosystems).Preferably, the Protein A resin is an agarose-based resin, i.e.,MabSelect SuRe resin. All three resin types are resistant to highconcentrations of guanidinium hydrochloride, urea, reducing agents andlow pH.

The column bed height employed at large scale is between 10 and 30 cm,depending on the resin particle properties such as pore size, particlesize and compressibility. Preferably, the column bed height is about 25cm. Flow rate and column dimensions determine antibody residence time onthe column. In one embodiment, the linear velocity employed for ProteinA is about 150 to about 500 cm/hr, preferably about 200 cm/h to about400 cm/h, more preferably about 200 cm/h to about 300 cm/h, and mostpreferably about 250 cm/h. Dynamic binding capacity ranges from 15-50 gof antibody per liter of resin, and depends on the flow rate, theparticular antibody to be purified, as well as the Protein A matrixused. Preferably, the column is loaded with no more than 45 g ofantibody per liter of resin. A method for determining dynamic bindingcapacities of Protein A resins has been described by Fahmer et al.Biotechnol Appl BioChem. 30:121-128 (1999). A lower loading flow ratemay increase antibody residence time and promote higher bindingcapacity. It also results in a longer processing time per cycle,requires fewer cycles and consumes less buffer per batch of harvestedcell culture fluid.

Other exemplary approaches to affinity purification include lectinaffinity chromatography, which can be performed in flow-through mode(product with undesired glycosylation binds to support while productwithout undesired glycosylation passes through the support) or bind &elute mode (product with desired glycosylation binds to support whileproduct without desired glycosylation passes through the support).

Proteins expressed in lower eukaryotes. e.g., P. pastoris, can bemodified with O-oligosaccharides solely or mainly composed of mannose(Man) residues. Additionally, proteins expressed in lower eukaryotes,e.g., P. pastoris, can be modified with N-oligosaccharides.N-glycosylation in P. pastoris and other fungi is different than inhigher eukaryotes. Even within fungi, N-glycosylation differs. Inparticular, the N-linked glycosylation pathways in P. pastoris aresubstantially different from those found in S. cerevisiae, with shorterMan(alpha 1,6) extensions to the core Man8GN2 and the apparent lack ofsignificant Man(alpha 1,3) additions representing the major processingmodality of N-linked glycans in P. pastoris. In some respects. P.pastoris may be closer to the typical mammalian high-mannoseglycosylation pattern. Moreover. Pichia and other fungi may beengineered to produce “humanized glycoproteins”(i.e., genetically modifyyeast strains to be capable of replicating the essential glycosylationpathways found in mammals, such as galactosylation.

Based on the desired or undesired O-linked and/or N-linked glycosylationmodification of a protein product, one or more lectins can be selectedfor affinity chromatography in flow-through mode or bind & elute mode.For example, if a desired recombinant protein lacks particular O-linkedand/or N-linked mannose modifications (i.e., desired protein isunmodified), a lectin that binds to mannose moieties, e.g., Con A. LCH.GNA, DC-SIGN and L-SIGN, can be selected for affinity purification inflow-through mode, such that the desired unmodified product passesthrough the support and is available for further purification orprocessing. Conversely, if a desired recombinant protein containsparticular O-linked and/or N-linked mannose modifications (i.e., desiredprotein is unmodified), a lectin that binds to mannose moieties, e.g.,Con A, LCH, GNA, DC-SIGN and L-SIGN, can be selected for affinitypurification in bind & elute mode, such that the desired modifiedproduct binds to the support and the undesired unmodified product passesthrough. In the later example, the flow through can be discarded whilethe desired modified product is eluted from the support for furtherpurification or processing. The same principle applies to recombinantprotein products containing other glycosylation modifications introducedby the fungal expression system.

Another pseudo-affinity purification tool is ‘mixed-mode’chromatography. As used herein, the term “mixed mode chromatography”refers to chromatographic methods that utilize more than one form ofinteractions between the stationary phase and analytes in order toachieve their separation, e.g., secondary interactions in mixed modechromatography contribute to the retention of the solutes. Advantages ofmixed mode chromatography include high selectivity, e.g., positive,negative and neutral substances could be separated in a single run, andhigher loading capacity.

Mixed mode chromatography can be performed on ceramic or crystallineapatite media, such as hydroxyapatite (HA) chromatography andfluoroapatite (FA) chromatography. Other mixed mode resins include, butare not limited to. CaptoAdhere. Capto MMC (GE Healthcare); HEAHypercel, and PPA Hypercel (Pall); and Toyopearl MX-Trp-650M (TosohBioScience). These chromatography resins provide biomolecule selectivitycomplementary to more traditional ion exchange or hydrophobicinteraction techniques.

Ceramic hydroxyapatite (Ca₅(PO₄)₃OH)₂ is a form of calcium phosphatethat can be used for the separation and purification of proteins,enzymes, nucleic acids, viruses and other macromolecules. Hydroxyapatitehas unique separation properties and excellent selectivity andresolution. For example, it often separates proteins that appear to behomogeneous by other chromatographic and electrophoretic techniques.Ceramic hydroxyapatite (CHT) chromatography with a sodium chloride orsodium phosphate gradient elution may be used as polishing step inmonoclonal antibody purification processes to remove dimers, aggregatesand leached Protein A.

Exemplary hydroxyapatite (HA) sorbents of type I and type II areselected from ceramic and crystalline materials. HA sorbents areavailable in different particle sizes (e.g. type 1, Bio-RadLaboratories). In an exemplary embodiment, the particle size of the HAsorbent is between about 10 μm and about 200 μm, between about 20 μm andabout 100 μm or between about 30 μm and about 50 μm. In a particularexample, the particle size of the HA sorbent is about 40 μm (e.g., CHT.Type 1).

Exemplary type 1 and type 11 fluoroapatite (FA) sorbents are selectedfrom ceramic (e.g., bead-like particles) and crystalline materials.Ceramic FA sorbents are available in different particle sizes (e.g. type1 and type 2, Bio-Rad Laboratories). In an exemplary embodiment theparticle size of the ceramic FA sorbent is from about 20 μm to about 180μm, preferably about 20 to about 100 μm, more preferably about 20 μm toabout 80 μm. In one example, the particle size of the ceramic FA mediumis about 40 μm (e.g., type 1 ceramic FA). In another example, the FAmedium includes HA in addition to FA.

The selection of the flow velocity used for loading the sample onto thehydroxyapatite or fluoroapatite column, as well as the elution flowvelocity depends on the type of hydroxyapatite or fluoroapatite sorbentand on the column geometry. In one exemplary embodiment, at processscale, the loading flow velocity is selected from about 50 to about 900cm/h, from about 100 to about 500 cm/h, preferably from about 150 toabout 300 cm/h and, more preferably, about 200 cm/h. In an exemplaryembodiment, the pH of the elution buffer is selected from about pH 5 toabout pH 9, preferably from about pH 6 to about pH 8, and morepreferably about pH 6.5.

In one embodiment, the disclosed purification processes employhydroxyapatite (HA) chromatography on CHT resin after protein Achromatography. Preferably, the elution is performed as a lineargradient (0-100%) from about 0 M to 1.5 M sodium chloride in a 5 mMsodium phosphate buffer at pH 6.5. The OD₂₈₀ of the effluent can bemonitored. In one embodiment, during elution, a single fraction from 0.1OD on the front flank to the peak maximum is collected and then a seriesof fractions, e.g., about one-third of the column volume, are collectedfrom the peak maximum to 0.1 OD on the rear flank are collected forfurther purity analysis. In another preferred embodiment, the elution isperformed as a linear gradient (0-100%) from about 5 mM to 0.25 M sodiumphosphate buffer at pH 6.5. The OD₂₈₀ of the effluent can be monitored.During elution, fractions of ˜½ CV can be collected from 0.1 OD on thefront flank to 0.1 OD on the rear flank for further purity analysis.

Polyclonal antibodies (e.g., serum samples) require antigen-specificaffinity purification to prevent co-purification of non-specificimmunoglobulins. For example, generally only 2-5% of total IgG in mouseserum is specific for the antigen used to immunize the animal. Thetype(s) and degree of purification that are necessary to obtain usableantibody depend upon the intended application(s) for the antibody.However, monoclonal antibodies that were developed using cell lines,e.g., hybridomas or recombinant expression systems, and produced asascites fluid or cell culture supernatant can be fully purified withoutusing an antigen-specific affinity method because the target antibody is(for most practical purposes) the only immunoglobulin in the productionsample.

Monitoring for Impurities

Profiling of impurities in biopharmaceutical products and theirassociated intermediates and excipients is a regulatory expectation.See, e.g., US Food and Drug Administration Genotoxic and CarcinogenicImpurities in Drug Substanmces and Products: Recommended Approaches.This guidance provides recommendations on how to evaluate the safety ofthese impurities and exposure thresholds. The European MedicinesAgency's (EMEA committee for Medicinal Products for Human Use (CHMP)also published the Guideline on the Limits of Genotoxic Impurities,which is being applied by European authorities for new drug products andin some cases also to drug substances in drug development. Theseguidelines augment the International Conference on Harmonization (ICH)guidances for industry: Q3A(R2) Impurities in New Drug Substances,Q3B(R2) Impurities in New Drug Producs, and Q3C(R3) Impurities: ResidualSolvents that address impurities in a more general approach.

Although some impurities are related to the drug product (i.e.,product-associated variant), others are added during synthesis,processing, and manufacturing. These impurities fall into several broadclasses: product-associated variants; process-related substancesintroduced upstream; residual impurities throughout the process;process-related residual impurities introduced downstream; and residualimpurities introduced from disposables.

As used herein, “product-associated variant” refers to a product otherthan the desired product (e.g., the desired multi-subunit complex) whichis present in a preparation of the desired product and related to thedesired product. Exemplary product-associated variants include truncatedor elongated peptides, products having different glycosylation than thedesired glycosylation (e.g., if an aglycosylated product is desired thenany glycosylated product would be considered to be a product-associatedvariant), complexes having abnormal stoichiometry, improper assembly,abnormal disulfide linkages, abnormal or incomplete folding,aggregation, protease cleavage, or other abnormalities. Exemplaryproduct-associated variants may exhibit alterations in one or more ofmolecular mass (e.g., detected by size exclusion chromatography),isoelectric point (e.g., detected by isoelectric focusing),electrophoretic mobility (e.g., detected by gel electrophoresis),phosphorylation state (e.g., detected by mass spectrometry), charge tomass ratio (e.g., detected by mass spectrometry), mass or identity ofproteolytic fragments (e.g., detected by mass spectrometry or gelelectrophoresis), hydrophobicity (e.g., detected by HPLC), charge (e.g.,detected by ion exchange chromatography), affinity (e.g., in the case ofan antibody, detected by binding to protein A, protein G, and/or anepitope to which the desired antibody binds), and glycosylation state(e.g., detected by lectin binding affinity). Where the desired proteinis an antibody, the term product-associate variant may include aglyco-heavy variant and/or half antibody species (described below).

Exemplary product-associated variants include variant forms that containaberrant disulfide bonds. For example, most IgG1 antibody molecules arestabilized by a total of 16 intra-chain and inter-chain disulfidebridges, which stabilize the folding of the IgG domains in both heavyand light chains, while the inter-chain disulfide bridges stabilize theassociation between heavy and light chains. Other antibody typeslikewise contain characteristic stabilizing intra-chain and inter-chaindisulfide bonds. Further, some antibodies (including Ab-A disclosedherein) contain additional disulfide bonds referred to as non-canonicaldisulfide bonds. Thus, aberrant inter-chain disulfide bonds may resultin abnormal complex stoichiometry, due to the absence of a stabilizingcovalent linkage, and/or disulfide linkages to additional subunits.Additionally, aberrant disulfide bonds (whether inter-chain orintra-chain) may decrease structural stability of the antibody, whichmay result in decreased activity, decreased stability, increasedpropensity to form aggregates, and/or increased immunogenicity.Product-associated variants containing aberrant disulfide bonds may bedetected in a variety of ways, including non-reduced denaturingSDS-PAGE, capillary electrophoresis, cIEX, mass spectrometry (optionallywith chemical modification to produce a mass shift in free cysteines),size exclusion chromatography, HPLC, changes in light scattering, andany other suitable methods known in the art. See, e.g., The ProteinProtocols Handbook 2002, Part V, 581-583, DOI:10.1385/1-59259-169-8:581.

Generally, dialysis, desalting and diafiltration can be used to exchangeantibodies into particular buffers and remove undesired low-molecularweight (MW) components. In particular, dialysis membranes,size-exclusion resins, and diafiltration devices that featurehigh-molecular weight cut-offs (MWCO) can be used to separateimmunoglobulins (>140 kDa) from small proteins and peptides. See, e.g.,Grodzki, A. C. and Berenstein, E. (2010). Antibody purification:ammonium sulfate fractionation or gel filtration. In: C. Oliver and M.C. Jamur (eds.), Immunocytochemical Methods and Protocols, Methods inMolecular Biology, Vol. 588:15-26. Humana Press.

Size-exclusion chromatography can be used to detect antibody aggregates,monomer, and fragments. In addition, size-exclusion chromatographycoupled to mass spectrometry may be used to measure the molecularweights of antibody; antibody conjugates, and antibody light chain andheavy chain.

Exemplary size exclusion resins for use in the purification and puritymonitoring methods include TSKgel G3000SW and TSKgel G3000SWx1 fromTosoh Biosciences (Montgomeryville, Pa., USA); Shodex KW-804,Protein-Pak 300SW, and BioSuite 250 from Waters (Milford, Mass., USA);MAbPac™ SEC-1 and MAbPac TM SCX-10 from Thermo Scientific (Sunnyvale,Calif. USA).

In one embodiment, size exclusion chromatography is used to monitorimpurity separation during the purification process. By way of example,an equilibrated TSKgel GS3000SW 17.8×300 mm column connected with aTSKgel Guard SW×16×40 mm from Tosoh Bioscience (King of Prussia, Pa.)may be loaded with sample, using a SE-HPLC buffer comprising 100 mMsodium phosphate, 200 mM sodium chloride pH 6.5 as a mobile phase with aflow rate of 0.5 mL/min in isocratic mode. Using an Agilent (SantaClara, Calif.) 1200 Series HPLC with UV detection instrument, absorbanceat UV 215 nm can be monitored. Samples can then be collected and dilutedto a desired concentration, e.g., 1 mg/mL. The diluted sample of afraction thereof, e.g., 30 μL, can then be loaded onto the SE-HPLCcolumn. Preferably, column performance is monitored using gel filtrationstandards (e.g., BioRad).

Product-associated variants include glycovariants. As used herein,“glycovariant” refers to a glycosylated product-associated variantsometimes present in antibody preparations and which contains at least apartial Fe sequence. The glycovariant contains glycans covalentlyattached to polypeptide side chains of the desired protein. Theglycovariant may be “glyco-heavy” or “glyco-light” in comparison to thedesired protein product, i.e., contains additional glycosylationmodifications compared to the desired protein or contains lessglycosylation modifications than the desired protein, respectively.Exemplary glycosylation modifications include, but are not limited to,N-linked glycosylation. O-linked glycosylation, C-glycosylation andphosphoglycosylation.

The glycovariant is characterized by increased or decreasedelectrophoretic mobility observable by SDS-PAGE (relative to a normalpolypeptide chain), lectin binding affinity, binding to an anti-Feantibody, and apparent higher or lower molecular weight of antibodycomplexes containing the glycovariant as determined by size exclusionchromatography. See, e.g., U.S. Provisional Application Ser. No.61/525,307, filed Aug. 31, 2011, which is incorporated by referenceherein in its entirety.

As used herein “glycosylation impurity” refers to a material that has adifferent glycosylation pattern than the desired recombinant protein.The glycosylation impurity may contain the same or different primary,secondary, tertiary and/or quaternary structure as the desiredrecombinant protein. Therefore, a glycovariant is a type ofglycosylation impurity.

Analytical methods for monitoring glycosylation of mAbs are importantbecause bioprocess conditions can cause, e.g., variation in high mannosetype, truncated forms, reduction of tetra-antennary and increase in tri-and biantennary structures, less sialyated glycans and lessglycosylation. The presence of glycovariants in a sample may bemonitored using analytical means known in the art, such as glycanstaining or labeling, glycoproteome and glycome analysis by massspectrometry and/or glycoprotein purification or enrichment. In oneembodiment, glycovariants are analyzed using lectin kinetic bindingassays, e.g., light interferometry (which may be performed using aForteBio Octet®), dual polarization interferometry (which may beperformed using a Farfield AnaLight®), static light scattering (whichmay be performed using a Wyatt DynaPro NanoStar™), dynamic lightscattering (which may be performed using a Wyatt DynaPro NanoStar™),composition-gradient multi-angle light scattering (which may beperformed using a Wyatt Calypso II), surface plasmon resonance (whichmay be performed using ProteOn XPR36 or Biacore T100), ELISA,chemoelectroluminescent ELISA, far western analysis, chemoluminescence(which may be performed using a MesoScale Discovery) or other lectinkinetic binding assay.

In one embodiment, glycan staining or labeling is used to detectglycovariants. For example, glycan sugar groups can be chemicallyrestructured with periodic acid to oxidize vicinal hydroxyls on sugarsto aldehydes or ketones so that they are reactive to dyes, e.g.,periodic acid-Schiff (PAS) stain, to detect and quantify glycoproteinsin a given sample. Periodic acid can also be used to make sugarsreactive toward crosslinkers, which can be covalently bound to labelingmolecules (e.g., biotin) or immobilized support (e.g., streptavidin) fordetection or purification.

In another embodiment, mass spectrometry is used to identify andquantitate glycovariants in a sample. For example, enzymatic digestionmay be used to release oligosaccharides from the immunoglycoprotein,where the oligosaccharide is subsequently derivatized with a fluorescentmodifier, resolved by normal phase chromatography coupled withfluorescence detection, and analyzed by mass spectrometry (e.g.,MALDI-TOF). The basic pipeline for glycoproteomic analysis includesglycoprotein or glycopeptides enrichment, multidimensional separation byliquid chromatography (LC), tandem mass spectrometry and data analysisvia bioinformatics.

Spectrometric analysis can be performed before or after enzymaticcleavage of glycans by, e.g., endoglycanase H (endo H) orpeptide-N4-(N-acetyl-beta-glucosaminyl)asparagine amidase (PNGase),depending on the experiment. Additionally, quantitative comparativeglycoproteome analysis may be performed by differential labeling withstable isotope labeling by amino acids in cell culture (SILAC) reagents.Moreover, absolute quantitation by selected reaction monitoring (SRM)can be performed on targeted glycoproteins using isotopically labeled,“heavy” reference peptides.

In one embodiment, lectins are used to detect and analyze glycovariantsof the desired recombinant protein during the purification process.Lectins are glycan-binding proteins have high specificity for distinctsugar moieties. A non-limiting list of commercially available lectins isprovided in Table 3 below.

TABLE 3 Exemplary commercially available lectins. Lectin Symbol LectinName Source Ligand motif Mannose binding lectins ConA Concanavalin ACanavalia α-D-mannosyl and α-D-glucosyl residues ensiformis branchedα-mannosidic structures (high α- mannose type, or hybrid type andbiantennary complex type N-Glycans) LCH Lentil lectin Lens culinarisFucosylated core region of bi- and triantennary complex type N-GlycansGNA Snowdrop Galanthus α 1-2, α 1-3 and α 1-6 linked high mannose lectinnivalis structures DC-SIGN Dendritic Cell- Human Calcium-dependentmannose-type Specific Murine carbohydrates Intercellular adhesionmolecule-3- Grabbing Non- integrin L-SIGN Liver/lymph HumanCalcium-dependent mannose-type node-specific Murine carbohydratesintercellular adhesion molecule-3- grabbing integrinGalactose/N-acetylgalactosamine binding lectins RCA Ricin, RicinusRicinus Galβ1-4GlcNAcβ1-R communis communis Agglutinin, RCA 120 PNAPeanut Arachis Galβ1-3GalNAcα1-Ser/Thr (T-Antigen) agglutinin hypogaeaAIL Jacalin Artocarpus (Sia)Galβ1-3GalNAcα1-Ser/Thr (T-Antigen)integrifolia VVL Hairy vetch Vicia villosa GalNAcα-Ser/Thr (Tn-Antigen)lectin N-acetylglucosamine binding lectins WGA Wheat Germ TriticumGlcNAcβ1-4GlcNAcβ1-4GlcNAc, Neu5Ac Agglutinin, vulgaris (sialic acid)WGA N-acetylneursminic acid binding lectins SNA Elderberry Sambucusnigra Neu5Acα2-6Gal(NAc)-R lectin MAL Maackia MaackiaNeu5Ac/Gcα2,3Galβ1,4Glc(NAc) amurensis amurensis leukoagglutinin MAHMaackia Maackia Neu5Ac/Gcα2,3Galβ1,3(Neu5Acαa2,6)GalNac amurensisamurensis hemoagglutinin Fucose binding lectins UEA Ulex europaeus Ulexeuropaeus Fucα1-2Gal-R agglutinin AAL Aleuria aurantia lectin AleuriaFucα1-2Galβ1-4(Fucα1-3/4)Galβ1-4GlcNAc, aurantiaR2-GlcNAcβ1-4(Fucα1-6)GlcNAc-R1

In one embodiment, a sample obtained from the fermentation process,e.g., during the run or after the run is completed, is subject to lectinbinding assay to detect the amount and/or type of glycosylatedimpurities in the sample(s). Similarly, in other embodiments, thepurification process includes detecting the amount and/or type ofglycosylated impurities in a sample from which the desired recombinantprotein is purified. For example, in a particular embodiment, a portionof the eluate or a fraction thereof from at least one chromatographicstep in the purification process may be contacted with a lectin.

The level of lectin binding often correlates with the level of theproduct-associated glycovariant impurity present in the eluate or afraction thereof (based on conventional size exclusion chromatographymethods), such that one or more fractions of the eluate can be selectedfor further purification and processing based on the content ofglycovariant impurities, e.g., select fractions of the eluate with lessthan 10⁰/o glycovariant for further chromatographic purification. Insome embodiments, multiple lectins (i.e., two or more lectins) may beused to monitor purity of the product associated glycovariantimpurities.

In an alternate embodiment, certain samples or eluate or fractionsthereof are discarded based on the amount and/or type of detectedglycosylated impurities. In yet another embodiment, certain samples orfractions are treated to reduce and/or remove the glycosylatedimpurities based on the amount and/or type of detected glycosylatedimpurities. Exemplary treatment includes one or more of the following:(i) addition of an enzyme or other chemical moiety that removesglycosylation. (ii) removal of the glycosylated impurities by effectingone or more lectin binding steps, (iii) effecting size exclusionchromatography to remove the glycosylated impurities.

In a particular embodiment, the lectin is conjugated to a probe and thenimmobilized to a support. See. FIG. 2. The support may be in batch orpacked into a column, e.g., for HIPLC. Exemplary probes include biotin,alkaline phosphatase (AP), horseradish peroxidase (HRP), luciferase,fluorescein (fluorescein isothiocyanate, FITC) and rhodamine(tetramethyl rhodamine isothiocyanate. TRITC), green fluorescent protein(GFP) and phycobiliproteins (e.g., allophycocyanin, phycocyanin,phycoerythrin and phycoerythrocyanin). Exemplary supports includeavidin, streptavidin, NeutrAvidin (deglycosylated avidin) and magneticbeads. It should be noted that the invention is not limited by couplingchemistry. Preferably, the lectin is biotinylated and immobilized onto astreptavidin sensor.

Standard protein-protein interaction monitoring processes may be used toanalyze the interaction between lectin and glycosylation impurities insamples from various steps of the purification process. Exemplaryprotein-protein interaction monitoring process include, but are notlimited to, light interferometry (which may be performed using aForteBio Octet®), dual polarization interferometry (which may beperformed using a Farfield AnaLight®), static light scattering (whichmay be performed using a Wyatt DynaPro NanoStar™), dynamic lightscattering (which may be performed using a Wyatt DynaPro NanoStar™),composition-gradient multi-angle light scattering (which may beperformed using a Wyatt Calypso II), surface plasmon resonance (whichmay be performed using ProteOn XPR36 or Biacore T100), ELISA,chemoelectroluminescent ELISA, far western analysis, chemoluminescence(which may be performed using a MesoScale Discovery) or other lectinkinetic binding assay.

Light interferometry is an optical analytical technique that analyzesthe interference pattern of white light reflected from two surfaces (alayer of immobilized protein on the biosensor tip, and an internalreference layer) to measure biomolecular interactions in real-time basedon a shift in the interference pattern (i.e., caused by a change in thenumber of molecules bound to the biosensor tip), thereby providinginformation about binding specificity, rates of association anddissociation, or concentration.

Dual polarization interferometry is based on a dual slab wave guidesensor chip that has an upper sensing wave guide as well as a loweroptical reference wave guide lit up with an alternating orthogonalpolarized laser beam. Two differing wave guide modes arecreated-specifically, the transverse Magnetic™ mode and the transverseelectric (TE) mode. Both modes generate an evanescent field at the topsensing wave guide surface and probe the materials that contact withthis surface. As material interacts with the sensor surface, it leads tophase changes in interference fringes. Then, the interference fringepattern for each mode is mathematically resolved into RI and thicknessvalues. Thus, the sensor is able to measure extremely subtle molecularchanges on the sensor surface.

Static light scattering (SLS) is a non-invasive technique whereby anabsolute molecular mass of a protein sample in solution may beexperimentally determined to an accuracy of better than 5% throughexposure to low intensity laser light (690 nm). The intensity of thescattered light is measured as a function of angle and may be analyzedto yield the molar mass, root mean square radius, and second virialcoefficient (A2). The results of an SLS experiments can be used as aquality control in protein preparation (e.g. for structural studies) inaddition to the determination of solution oligomeric state(monomer/dimcr etc.). SLS experiments may be performed in either batchor chromatography modes.

Dynamic light scattering (also known as quasi-elastic light scattering.QELS, or photon correlation spectroscopy. PCS) is a technique formeasuring the hydrodynamic size of molecules and submicron particlesbased on real-time intensities (compared to time-average intensities, asmeasured by static light scattering). Fluctuations (temporal variation,typically in a us to ms time scale) of the scattered light from aparticle in a medium are recorded and analyzed in correlation delay timedomain. The particles can be solid particles (e.g., metal oxides,mineral debris, and latex particles) or soft particles (e.g., vesiclesand micelles) in suspension, or macromolecular chains (e.g., syntheticpolymers and biomaterials) in solution. Since the diffusion rate ofparticles is determined by their sizes in a given environment,information about their size is contained in the rate of fluctuation ofthe scattered light.

The scattering intensity of a small molecule is proportional to thesquare of the molecular weight. As such, dynamic and static lightscattering techniques are very sensitive to the onset of proteinaggregation and other changes in protein structure arising from subtlechanges in conditions.

Composition-gradient multi-angle light scattering (CG-MALS) employs aseries of unfractionated samples of different composition orconcentration in order to characterize macromolecular interactions suchas reversible self- and hetero-association of proteins, reaction ratesand affinities of irreversible aggregation, or virial coefficients. Suchmeasurements provide information about specific reversible complexbinding (e.g., K_(d), stoichiometry, self and/or heteroassociations),non-specific interactions (e.g., self- and cross-virial coefficients),aggregation and other time-dependent reactions (e.g., stop-flow kineticsand t) and Zimm plots (e.g., concentration gradients for determiningM_(W), A₂, A₃ (second and third virial coefficients), or r_(g)).

The surface plasmon resonance (SPR) phenomenon occurs when polarizedlight, under conditions of total internal reflection, strikes anelectrically conducting (e.g., gold) layer at the interface betweenmedia of different refractive index (i.e., glass of a sensor surface(high refractive index) and a buffer (low refractive index)). A wedge ofpolarized light, covering a range of incident angles, is directed towardthe glass face of the sensor surface. An electric field intensity (i.e.,evanescent wave), which is generated when the light strikes the glass,interacts with, and is absorbed by, free electron clouds in the goldlayer, generating electron charge density waves called plasmons andcausing a reduction in the intensity of the reflected light. Theresonance angle at which this intensity minimum occurs is a function ofthe refractive index of the solution close to the gold layer on theopposing face of the sensor surface. Reflected light is detected withina monitoring device, e.g., ProteOn XPR36 or Biacore system. The kinetics(i.e. rates of complex formation (k_(a)) and dissociation (k_(d))),affinity (e.g., K_(D)), and concentration information can be determinedbased on the plasmon readout.

Information obtained from these and other protein-protein interactionmonitoring processes can be used to, e.g., quantify binding affinity andstoichiometry of enzyme/inhibitor or antibody/antigen interactions orglycoprotein/lectin interactions; study the impact of small molecules onprotein-protein interactions; adjust buffer parameters to improveformulation stability and viscosity; optimize antibody purification andunderstand the effects of large excipients on formulations; quantifyimpact of solvent ionic strength, pH, or excipients on polymerization orprotein associations; measure kinetics of self-assembly and aggregation;and characterize macromolecular binding affinity and associated complexstoichiomctry over a wide range of buffer compositions, time, andtemperature scales.

In a preferred embodiment, the level of lectin binding (which correlateswith the amount of glycovariant impurity) is determined using lightinterferometry. e.g., Octet analysis instruments (FortéBIO).

Exemplary process-related impurities introduced upstream include nucleicacids (e.g., DNA and RNA) and host cell proteins (HCP) that are unwantedcell components found with the protein of interest after cell lysis.These process-related impurities also include antibiotics that are addedupstream to the cell-culture media to control bacterial contaminationand maintain selective pressure on the host organisms. Exemplaryantibiotics include kanamycin, ampicillin, penicillin, amphotericin B,tetracyline, gentamicin sulfate, hygromycin B, and plasmocin.

Exemplary residual impurities incurred throughout the process includeprocess enhancing agents or catalysts, which are added throughout theprocess to make some of the steps more efficient and increase yield ofthe product. For example, guanidine and urea are added forsolubilization of the fermentation output, and glutathione anddithiothreitol (DTT) are used during reduction and refolding ofproteins.

Exemplary process-related impurities introduced downstream includechemicals and reagents (e.g., alcohols and glycols) required forchromatographic purification of target proteins that must be clearedfrom the process, as well as surfactants (e.g., Triton-X, Pluronic,Antifoam-A, B, C, Tween, or Polysorbate) that are added duringdownstream processing to aid in separating the protein, peptide, andnucleic acids from the process stream by lowering the interfacialtension by adsorbing at the liquid-liquid interface.

Exemplary residual impurities introduced from disposables include“extractables,” which are compounds that can be extracted from acomponent under exaggerated conditions (e.g., harsh solvents or atelevated temperatures) and have the potential to contaminate the drugproduct, and “leachables,” which are compounds that leach into the drugproduct formulation from the component as a result of direct contactwith the formulation under normal conditions or sometimes at acceleratedconditions. Leachables may be a subset of extractables. Extractablesmust be controlled to the extent that components used are appropriate.Leachables must be controlled so that the drug products are notadulterated.

To further articulate the invention described above, we provide thefollowing non-limiting examples.

EXAMPLES

The following examples are put forth so as to provide those of ordinaryskill in the art with a complete disclosure and description of how tomake and use the subject invention, and are not intended to limit thescope of what is regarded as the invention. Efforts have been made toensure accuracy with respect to the numbers used (e.g. amounts,temperature, concentrations, etc.) but some experimental errors anddeviations should be allowed for. Unless otherwise indicated, parts areparts by weight, molecular weight is average molecular weight,temperature is in degrees centigrade; and pressure is at or nearatmospheric.

Example 1: Ab-A Purification and Recovery

This example illustrates that the purity of recombinant antibodiesgenerated in P. pastoris was improved by using a series of primaryrecovery and chromatographic purification processes. An overview of thepurification method is shown in FIG. 1. These methods can be used topurify and recover a variety of antigen-specific antibodies expressed indifferent systems.

P. pastoris cells containing stably integrated sequences encoding theAb-A heavy and light chains (corresponding to SEQ ID NO:54 and SEQ IDNO:52 as listed in US 20120294797, which is incorporated by reference inits entirety) linked to a secretion signal were cultured and antibodyexpression was induced.

Whole fermentation broth was treated with ethylene diamine tetraaceticacid (EDTA) to 3 mM final concentration and with a flocculating agent.Cells and flocculated debris were removed from the harvested broth bycentrifugation, followed by clarification through depth and 0.2 μmfilters.

The clarified broth was then applied to a column of MabSelect SuRe (GEHealthcare Life Sciences) resin to capture Ab-A by Protein A affinitychromatography. Chromatography was performed at ambient temperature. Acolumn of 25 cm bed height was sanitized with 0.1 M sodium hydroxide andthen equilibrated with 20 mM sodium phosphate. 150 mM sodium chloride,pH 6.0 buffer (“PrA equilibration buffer”) prior to loading. The columnwas loaded to a capacity of not more than 45 g Ab-A per L resin at 250cm/hr linear velocity, and then operated at the same linear velocitythroughout. Following application of the load, the column was rinsed for5 column volumes (CV) with equilibration buffer, and then washed for 5CV with 20 mM sodium phosphate, 10 mM EDTA, 1 M sodium chloride, pH 6.0to remove loosely bound materials. The column was rinsed with another 5CV equilibration buffer to remove wash components, and then bound Ab-Awas desorbed with 1 M arginine, pH 4.0 (“PrA elution buffer”). Theelution step was carried out as a linear gradient from 0-100% elutionbuffer over 3 CV followed by elution at 100% elution buffer for another3 CV. The OD₂₈₀ of the effluent was monitored, and eluate was collectedfrom 1 OD on the front flank to 1 OD on the rear flank. The eluate wascollected in a vessel pre-loaded with 0.15 CV of 1 M Tris, pH 8.0 (“PrAneutralization buffer”). Following collection the vessel's contents weremixed and its pH value determined, prior to final adjustment to pH 6.5using either 5% hydrochloric acid or 1 M sodium hydroxide as necessary.The neutralized eluate was 0.2 μm filtered, then forwarded on to thehydroxyapatite chromatography step. Following product elution, thecapture column was stripped with 20 mM sodium acetate, pH 3.6 for 3 CV,cleaned with 0.2 M sodium hydroxide for 3CV, and rinsed withequilibration buffer for 3 CV prior to storage in 20% ethanol.

Intermediate purification of Ab-A used mixed mode chromatography onceramic hydroxyapatite (CHT, Type 1, 40 μm) resin. This step was carriedout at ambient temperature and at not more than 200 cm/hr linearvelocity throughout. Prior to each run the column was sanitized using 3CV of 1 M sodium hydroxide, stripped with 3 CV 500 mM sodium phosphate,pH 6.5 (“strip buffer”), and equilibrated with at least 3 CV 5 mM sodiumphosphate, pH 6.5 (“CHT equilibration buffer”). The CHIT load wasprepared by diluting the filtered, neutralized capture eluate with CHTequilibration buffer to a conductivity of not more than 4 mS/cm. The CHTload was then applied to the equilibrated column after passing through a0.2 μm filter placed ahead of the column. Following loading, the columnwas washed with 5 CV of CHT equilibration buffer and then eluted with a20 CV linear gradient from 0-100⁰%5 mM sodium phosphate, 1.5 M sodiumchloride, pH 6.5 (“CHT elution buffer”). The ODaoof the effluent wasmonitored, and a single fraction from 0.1 OD on the front flank to thepeak maximum was collected. Thereafter, a series of fractions of ˜⅓^(rd)CV were collected from the peak maximum to 0.1 OD on the rear flank. Thefractions were analyzed for purity (see FIG. 3), and a set of contiguousfractions (including the first, larger fraction) were combined toachieve a CHT Pool of desired purity and reduced glycovariant content(see FIG. 4 and FIG. 5). After elution, the CHT column was stripped with3 CV 500 mM sodium phosphate. pH 6.5 (“CHT strip buffer”), cleaned inplace with 5 CV 1 M sodium hydroxide, and rinsed with 3 CV 0.1 M sodiumhydroxide storage solution.

Polish purification of Ab-A used hydrophobic interaction chromatography(HIC) on polypropylene glycol (PPG-) 600M resin. This step was carriedout at ambient temperature and at not more than 200 cm/hr linearvelocity throughout. Prior to each run the column was sanitized using 3CV of 0.5 M sodium hydroxide, stripped with 3 CV water, and equilibratedwith at least 3 CV 20 mM sodium phosphate, 0.7 M sodium sulfate, pH 7.0(“HIC equilibration buffer”). The HIC load was prepared by adjusting 0.2μm filtered CHT Pool to a conductivity of at least 77.5 mS/cm using 20mM sodium phosphate, 1.1 M sodium sulfate, pH 7.0 (“HIC dilutionbuffer”). The HIC load was then applied to the equilibrated column afterpassing through a 0.2 μm filter placed ahead of the column. Followingloading, the column was washed with 5 CV of HIC equilibration buffer andthen eluted with a 20 CV linear gradient from 0-100% 20 mM sodiumphosphate, pH 7.0 (“HIC elution buffer”). The OD₂₈₀ of the effluent wasmonitored, and a series of fractions of ˜⅓^(rd) CV were collected from0.1 OD on the front flank to 0.1 OD on the rear flank. The fractionswere analyzed for purity (see FIG. 6), and a set of contiguous fractionswere combined to form a HIC Pool of desired purity and reducedglycovariant content. After elution, the HIC column was stripped with 3CV water, cleaned in place with 6 CV 0.5 M sodium hydroxide (with a60-120 min pause between the first 3 and last 3 CV), rinsed with 3 CVwater, and transferred into 0.1 M sodium hydroxide storage solution.

Ab-A in the HIC Pool was formulated by ultrafiltration and diafiltration(UFDF) in a tangential flow filtration (TFF) system equipped with 30 kDamolecular weight cut-off membranes. The system was rinsed with water,tested for membrane integrity, sanitized, and equilibrated in aformulation buffer in preparation for loading with 0.2 μm filtered HICPool. Following loading, the solution was concentrated byultrafiltration and then exchanged into formulation buffer bydiafiltration versus 6-8 turnover volumes of formulation buffer. Theprotein solution was further concentrated in a second round ofultrafiltration and then the retentate was drained from the TFF system.The system was flushed with formulation buffer to recover residualprotein. The protein concentrations of the retentate and the flush weredetermined, and then appropriate portions of each were mixed and furtheradjusted with formulation buffer to achieve the desired final Ab-Aconcentration. The TFF product was 0.2 μm filtered into sterile bottlesin a biological safety cabinet, and stored at ≤−20° C. 100238 Productvariants in Ab-A preparations were visualized on protein gels (see FIG.7). Lanes 1 and 12: control lanes (IX sample buffer): lanes 2, 6 and 11:molecular weight markers; lanes 3-5: total sample loaded onto theProtein A affinity column; lane 7: Ab-A antibody preparation afterProtein A affinity chromatography; lane 8: Ab-A antibody preparationafter CHT chromatography; lane 9: Ab-A antibody preparation after HICchromatography; and lane 10: Ab-A antibody preparation after bulkfiltration (BDS). Because the samples were subjected to denaturing andreducing conditions (FIG. 7 panel A and panel B, respectively), thismethod can detect abnormalities affecting the constitution of individualantibody chains but would not be expected to detect other types ofabnormalities (such as improper stoichiometry, aggregation, improperdisulfide linkages, or other assembly errors). The antibody was purifiedby Protein-A affinity chromatography, CHT hydroxyapatite mixed modechromatography and PPG-600M hydrophobic interaction chromatography, asdescribed above, and a sample from different steps along thepurification scheme was resolved by SDS-PAGE and stained with CoomassieBlue. The major bands corresponded to the predicted molecular weight ofthe intact antibody on the non-reduced gel and to heavy and light chainsin the reduced gel. Several species of product-associated variants werereadily observable in each sample, the most prominent being alow-mobility variant (FIG. 7, arrow labeled “low-mobilityproduct-associated variant”). The low-mobility product-associatedvariant had decreased electrophoretic mobility relative to the heavychain. The amount of this product-associated variant was visibly reducedin the antibody preparation following purification using Protein-Aaffinity chromatography, C-IHT hydroxyapatite mixed mode chromatographyand PPG-600M hydrophobic interaction chromatography (sece FIG. 7,compare lanes 3-5 with lanes 7-10).

Antibody purity was also monitored using size-exclusion chromatography.(SE-HPLC) using an Agilent (Santa Clara, Calif.) 1200 Series HPLC withUV detection instrument. For sample separation, a TSKgel GS3000SWx17.8×300 mm column connected with a TSKgel Guard SWx1 6×40 mm from TosohBioscience (King of Prussia, Pa.) was used. A 100 mM sodium phosphate,200 mM sodium chloride pH 6.5 was used as mobile phase with a flow rateof 0.5 mL/min in isocratic mode and absorbance at UV 215 nm wasmonitored. Before injection of samples the column was equilibrated untila stable baseline was achieved. Samples were diluted to a concentrationof 1 mg/mL using mobile phase and a 30 μL volume was injected. Tomonitor column performance, BioRad (Hercules, Calif.) gel filtrationstandards were used.

Purification results are presented in Table 4. In particular. Ab-Aproduct as well as low molecular weight (LMW), aggregate andglycovariant (GV) impurities were monitored after Protein-A affinitychromatography, CHT hydroxyapatite mixed mode chromatography, PPG-600Mhydrophobic interaction chromatography and UF/DF 30 kDa filterformulation and fill. With every stage of the purification process,there were increasingly reduced levels (%) of each impurity that wasmonitored, resulting in Ab-A product with at least 98% purity.

TABLE 4 Quantitative assessment of Ab-A purity throughout thepurification method. Percentage of aggregate, variant, Ab-A and low-mobility product-associated variant after Protein-A affinitychromatography, CHT hydroxyapatite mixed mode chromatography, PPG-600Mhydrophobic interaction chromatography and UP/DF formulation and fill isshown for three different purification preparations of Ab-A. % % % %Low- Aggregate Variant Ab-A molecular weight Purification 1 Protein AEluate 3.6 3.8 88.5 4.2 CHT 0.6 0.7 95.4 7.5 PPG 0.3 0.6 98.2 0.9 UFDFProduct 0.1 0.6 98.1 1.2 Purification 2 Protein A Eluate 2.1 9.6 86.91.4 CHT Pool 0.6 0.7 97,7 1.1 PPG Pool 0.2 0.6 98.4 0.8 UFDF Product 0.20.6 98.3 0.9 Purification 3 Protein A Eluate 3.4 11.8 83.1 1.7 CHT Pool0.2 0.7 97.8 1.4 PPG Pool 0.4 0.7 98.1 0.8 UFDF Product 0.2 0.7 99.1 0.1

Additional process-related impurity monitoring was performed toquantitate clearance of host cell proteins, residual Protein A, dsDNAand glycans (e.g., l-D-glucan) as a result of purification methods thatinclude a lectin-binding monitoring step. See, Table 5. Overall, thepurification scheme resulted in reduced levels of impurities in thepurified antibody sample.

TABLE 5 Quantitative assessment of process-related impurity clearanceprovided by the purification methods. The concentration (relative toantibody) of P. pastoris host cell protein (HCP), S. cerevisiae hostcell protein (HCP), residual Protein A, dsDNA and β-D-glucan afterProtein-A affinity chromatography, CHT hydroxyapatite mixed modechromatography, and PPG-600M hydrophobic interaction chromatography isshown for an exemplary purification preparation of Ab-A. P. pastoris S.cerevisiae Residual β-D- HCP HCP Protein A dsDNA glucan ppm ppm ppm ppmppb Protein A 5,942 132 8.5 1.4 19.5 CHT 2.1 9.4 <0.4 3.8 16.1 PPG <1.2<2.4 <0.4 2.8 16.3

Thus, the purification methods including chromatography andlectin-monitoring of impurities demonstrated improved antibody purity.In particular, the final product had greater than 98% purity followingProtein-A affinity chromatography, CHT hydroxyapatite mixed modechromatography and PPG-600M hydrophobic interaction chromatography.

Example 2: Quantitation of Glycoproteins

This example describes a binding assay to facilitate rapid and precisequantitation of glycoproteins in protein samples. These methods can beused to monitor and assess performance of protein expression and proteinpurification systems. The speed and reproducibility achievable withthese methods permit monitoring to occur in near real-time. Duringprotein purification, these methods can be used in multiple waysincluding identifying fractions which should be collected and optionallypooled, monitoring purification performance, and determining whether adesired level of purity has been achieved or alternatively whetheradditional or modified purification steps should be performed to achievethe desired level of purity. Similarly, when used to monitor performanceof a gene expression system these methods permit feedback control ofexpression system parameters in order to achieve the desired (e.g.,lower) level of glycoproteins.

Strepavidin Biosensors with Biotinylated Galanthus nivalis agglutininwere used to determine the concentration of glycovariants in solutionrelative to a standard. In particular, an Octet interferometer(ForteBio. Menlo Park, Calif.) with Streptavidin Biosensors (ForteBio)functionalized with biotinylated Galanthus nivalis Lectin (GNL [alsoreferred to as GNA], Cat B-1245, Vector Labs. Burlingame, Calif.) wasused to determine the level of activity of a biomolecule in solutionrelative to a standard. Briefly, sensors were functionalized bypre-wetting in 1× kinetics buffer (a 1:10 dilution in Dulbecco'sPhosphate Buffered Saline of 10× kinetics buffer from Fortebio. Part No:18-5032) then immersed in a dilution of biotinylated GNL lectin andplaced on a shaking platform for a prescribed length of time.

Standards, unknowns and controls for measurement were diluted in IXkinetics buffer and arrayed in a black microtiter plate, with replicatesas appropriate. The plate with sample dilutions was read on the Octetusing the GNL-functionalized sensors and standard quantitation assaymethods (such as for Protein A sensors) as described by the manufacturer(ForteBio).

Data Analysis was performed with a ForteBio Analysis software module.Standard curve linearity and reproducibility of known samples wereevaluated. Well activity levels were appropriately adjusted for sampleconcentration/dilution factor to determine mass-normalized specificactivity levels, termed Relative Units (RU).

Sample storage and handling: Samples and standards were stored at 4° C.or −20° C. depending on existing stability data. While preparing theassay, samples were kept on ice. Kinetics buffers (Forte Bio Catalog No.18-5032, 10× and 1×, containing PBS+0.1% BSA, 0.02% Tween20 and 0.05%sodium azide) were stored at 4° C. GNL is stored at 4° C.

Functionalizing the sensors: Strepavidin sensors (Forte Bio Catalog No.18-5019, tray of 96 biosensors coated with strepavidin) were soaked in1× Kinetics buffer for at least 5 minutes. Biotinylated GNL was diluted1/1000 into 1× kinetics buffer to obtain the volume calculated in stepbelow. 1× kinetics buffer was prepared from 10× kinetics buffer andHyclone DPBS+Ca+Mg. 120 ul of kinetics buffer was aliquoted per well foreach sensor needed into a half area black plate, e.g., 96-Well BlackHalf Area Plates Medium & High Binding (Greiner Bio-One Cat 675076 orVWR Cat 82050-044). The sensors were transferred to plates withBiotinylated GNL, and the plates were incubated with shaking for atleast 30 minutes.

Preparation of the sensors and samples: Sensors were handled with amultichannel pipettor with particular care for the tips of the sensorssince damage (e.g., scraping) to these tips can affect the assayresults. A medium binding black plate was used for sensors with sensortray. A separate black plate was used for samples and standards. 150 μlwas added per well for unknowns, controls and standards. A media blankor a solution containing a known glycovariant concentration can beoptionally included as a control sample. A new sensor was used for eachstandard well of the assay. Each sensor was rinsed in 1× kinetics bufferbefore use. A duplicate 3-fold dilution series of 8 points wassufficient for a standard curve. The dilutions were made using 1×kinetics buffer. 1× kinetics buffer was also used as a blank sample.

The Octet conditions were set as follows: Quantitation Time (s) 250;Shake speed 1000 rpm. The plate was defined by assigning the samplewells and the sensors. In particular, the sample wells were assigned byselecting the wells corresponding to the samples and entering theiridentity, e.g., “unknown” to input a dilution factor or “standard” toinput a known concentration. The sensors were not reused for this assay.The program optionally included a delay and/or shaking before processingthe sample (e.g., plate was equilibrated to 30° C. while shaking at 200RPM for 300 seconds).

A different lectin, DC-SIGN (R&D Systems cat #161-DC-050) wasbiotinylated with LC-LC-biotin (Pierce cat #21338) and used tofunctionalize streptavidin sensors that were employed in a similar assayas described above.

The Octet lectin-binding assay described above was used to quantitatethe amount of glycosylated proteins present in fractions of the eluatecollected after hydroxyapatite mixed mode chromatography and afterhydrophobic interaction chromatography. In particular, Octet Activity(RU) values for binding to GNA and DC-SIGN were determined for each of21 fractions of the eluate collected after CHT hydroxyapatite mixed modechromatography and for each of 25 fractions of the eluate collectedafter PPG-600M hydrophobic interaction chromatography. See, FIG. 5,panel A and FIG. 6, panel A, respectively. For each fraction analyzed,the Octet Activity (RU) value was plotted against the concentration ofAb-A present in the same fraction. For CHT fractions, both GNA Octetvalues and DC-SIGN Octet values correlated well with relativeglycovariant concentration. See, FIG. 4.

Fractions of the column eluate were selected for further processingbased on the level of glycovariant impurities contained in the sample asdetermined using the Octet assays using either Baseline pooling criteriaor strict pooling criteria discussed in Example 1. In particular,following strict pooling criteria, fraction 1 through fraction 10 of theCHT hydroxyapatite mixed mode column were selected for furtherprocessing, whereas fraction 1 through fraction 13 were selected forfurther processing per Baseline pooling criteria. The strict pooledfractions had a 1.9 RU, compared to a 2.3 RU for the Baseline pooledfractions, as determined by GNA-Octet assay. The glycovariant impuritycontent as measured by Octet assay correlated with increased levels ofmonomannose, mannobiose and mannotriose in the Baseline criteria poolcompared to the strict criteria pool (i.e., 1.55 mol monomannose/molAb-A in the Stringent Pool compared to 1.60 mol monomannose/mol Ab-A inthe Baseline Pool, and 0.22 mol mannotriose/mol Ab-A in the StringentPool compared to 0.28 mol mannotriose/mol Ab-A in the Baseline Pool).See, FIG. 5, panel B.

Similarly, following strict pooling criteria, fraction 8 throughfraction 23 of the PPG-600M hydrophobic interaction column were selectedfor further processing, whereas fraction 4 through fraction 23 wereselected for further processing per Baseline pooling criteria. Thestrict pooled fractions had a 1.1 RU, compared to a 1.4 RU for theBaseline pooled fractions, as determined by GNA-Octet assay. Theglycovariant impurity content as measured by Octet assay correlated withincreased levels of monomannose, mannobiose and mannotriose in theBaseline criteria pool compared to the strict criteria pool (i.e., 1.57mol monomannose/mol Ab-A in the Stringent Pool compared to 1.48 molmonomannose/mol Ab-A in the Baseline Pool: 0.52 mol mannobiose/mol Ab-Ain the Stringent Pool compared to 0.14 mol mannobiose mol/Ab-A mol inthe Baseline Pool; and 0.32 mol mannotriose/mol Ab-A in the StringentPool compared to 0.07 mol mannotriose/mol Ab-A in the Baseline Pool).See, FIG. 6, panel B.

Thus, the quantitative lectin binding assay when used in combinationwith chromatographic purification methods improves antibody productpurity. Based on the level of lectin-binding activity, particularfractions of the eluate after different chromatography steps can beselected for further processing to increase the yield of the desiredantibody product and minimize the presence of unwanted impurities.

Example 3: Ab-B Purification and Recovery

This example illustrates that the purity of recombinant antibodiesgenerated in P, pastoris was improved by using a series of primaryrecovery and chromatographic purification processes. An overview of thepurification method is shown in FIG. 1. These methods can be used topurify and recover a variety of antigen-specific antibodies expressed indifferent systems.

P. pastoris cells containing stably integrated sequences encoding theAb-B heavy and light chains (corresponding to SEQ ID NO:681 and SEQ IDNO:701 as listed in US 20120294797, which is incorporated by referencein its entirety) were cultured and antibody expression was induced.

Whole broth was treated with ethylene diamine tetraacetic acid (EDTA) to3 mM final concentration and with a flocculating agent. Cells andflocculated debris were removed from the harvested broth bycentrifugation, and followed by clarification through depth and 0.2 μmfilters.

The clarified broth was applied to a column of MabSelect SuRe resin tocapture Ab-B by Protein A affinity chromatography. Chromatography wasperformed at ambient temperature. A column of 23 cm bed height wassanitized with 0.1 M sodium hydroxide and then equilibrated with 20 mMsodium phosphate, 150 mM sodium chloride, pH 6.0 buffer (“Pr Aequilibration buffer”) prior to loading. The column was loaded to atarget capacity of 25 g Ab-B per L resin at 250 cm/hr linear velocity,and then operated at the same linear velocity throughout. Followingapplication of the load, the column was rinsed for ≥3 column volumes(CV) with capture equilibration buffer to remove loosely boundmaterials. Bound Ab-B was then desorbed with ≥3 CV of 1 M arginine, pH4.0 elution buffer (“PrA elution buffer”). The OD₂₈₀ of the effluent wasmonitored, and eluate was collected from 1 OD on the front flank to 1 ODon the rear flank. The eluate was collected in a vessel pre-loaded with0.15 CV of 1 M Tris. pH 8.0 neutralization buffer (“PrA neutralizationbuffer”). Following collection the vessel's contents were mixed, and itspH value determined, prior to final adjustment to pH 6.5 using either 5%hydrochloric acid or 1 M sodium hydroxide as necessary. The neutralizedeluate was 0.2 μm filtered, then forwarded on to the hydroxyapatitechromatography step. Following product elution, the Protein A column wascleaned with 0.2 M sodium hydroxide for 3CV, and rinsed withequilibration buffer for 3 CV prior to storage in 20% ethanol.

Intermediate purification of Ab-B uses mixed mode chromatography onceramic hydroxyapatite (CHT, Type 1, 40 μm) resin. This step was carriedout at ambient temperature and at not more than 200 cm/hr linearvelocity throughout. Prior to running, the column was sanitized using 3CV of 1 M sodium hydroxide and equilibrated with at least 3 CV 5 mMsodium phosphate, pH 6.5 equilibration buffer (“CHT equilibrationbuffer”). The CHT load was prepared by diluting the filtered,neutralized capture eluate with CHT equilibration buffer to aconductivity of not more than 4 mS/cm. The CIIHT load was then appliedto the equilibrated column after passing through a 0.2 μm filter.Following loading, the column was washed with 5 CV of equilibrationbuffer and then eluted with a 20 CV linear gradient from 5 mM to 0.25 Msodium phosphate, pH 6.5 (“CHT elution buffer 2”). The OD₂₈₀ of theeffluent was monitored, and a series of fractions of ˜½ CV werecollected from 0.1 OD on the front flank to 0.1 OD on the rear flank.The fractions were analyzed for purity, and a set of contiguousfractions were combined to achieve a CHT Pool of desired purity andreduced glycovariant content (see FIG. 8). After elution, the CHT columnwas stripped with 5 CV 500 mM sodium phosphate. pH 6.5 strip buffer(“CHT strip buffer”), cleaned in place with 5 CV 1 M sodium hydroxide,and rinsed with 5 CV 20% ethanol storage solution.

Polish purification of Ab-B used hydrophobic interaction chromatography(HIC) on Phenyl High Performance (GE Healthcare) resin. This step wascarried out at ambient temperature and at not more than 200 cm/hr linearvelocity throughout. Prior to running, the column was sanitized using 3CV of 1 M sodium hydroxide, and equilibrated with 5CV 20 mM sodiumphosphate, 0.7 M sodium sulfate, pH 7.0 equilibration buffer (“HICequilibration buffer”). The HIC load was prepared by adjusting 0.2 μmfiltered CHT Pool to a conductivity ≥77.5 mS/cm using 20 mM sodiumphosphate. 1.1 M sodium sulfate. pH 7.0 HIC dilution buffer. The HICload was then applied to the equilibrated column after passing through a0.2 μm filter. Following loading, the column was washed with 5 CV of HICequilibration buffer and then eluted with a 20 CV linear gradient from0-100% 20 mM sodium phosphate, pH 7.0 (“HIC elution buffer”). The OD₂₈₀of the effluent was monitored, and a series of fractions of ˜⅓^(rd)CVwere collected from 0.1 OD on the front flank to 0.1 OD on the rearflank. The fractions were analyzed for purity (see FIG. 9), and a set ofcontiguous fractions were combined to form a HIC Pool of desired purityand reduced glycovariant content (see FIG. 8 and FIG. 9). After elution,the HIC column was stripped with 4 CV HIC elution buffer, cleaned inplace with ≥3 CV 1 M sodium hydroxide, and transferred into 0.1 M sodiumhydroxide storage solution.

Product variants in Ab-B preparations were visualized on protein gels(see FIG. 10). In both gels, lanes 1, 2 and 6 contain molecular weightmarkers; lane 3 contains Protein A eluate; lane 4 contains CHT pool; andlane 5 contains HIC pool. Because the samples were subjected todenaturing and reducing conditions (FIG. 10 panel A and panel B,respectively), this method can detect abnormalities affecting theconstitution of individual antibody chains but would not be expected todetect other types of abnormalities (such as improper stoichiometry,aggregation, improper disulfide linkages, or other assembly errors). Theantibody was purified by Protein-A affinity chromatography. CHThydroxyapatite mixed mode chromatography and Phenyl-Sepharose HighPerformance (HP) hydrophobic interaction chromatography, as describedabove, and a sample from different steps along the purification schemewas resolved by SDS-PAGE and stained with Coomassie Blue. The majorbands corresponded to the predicted molecular weight of the intactantibody on the non-reduced gel and to heavy and light chains in thereduced gel. Several species of product-associated variants were readilyobservable in each sample, the most prominent being a low-mobilityvariant (FIG. 10, arrow labeled “low-mobility product-associatedvariant”). The low-mobility product-associated variant had decreasedelectrophoretic mobility relative to the heavy chain. The amount of thisproduct-associated variant was visibly reduced in the antibodypreparation following purification using Protein-A affinitychromatography, CHT hydroxyapatite mixed mode chromatography and PhenylHIP hydrophobic interaction chromatography (see FIG. 10, compare lanes4-5 with lane 3).

Antibody purity was also monitored using size-exclusion chromatography.(SE-HPLC) using an Agilent (Santa Clara, Calif.) 1200 Series HPLC withIUV detection instrument. For sample separation, a TSKgel GS3000SWx17.8×300 mm column connected with a TSKgel Guard SWx1 6×40 mm from TosohBioscience (King of Prussia, Pa.) was used. A 100 mM sodium phosphate,200 mM sodium chloride pH 6.5 was used as mobile phase with a flow rateof 0.5 mL/min in isocratic mode and absorbance at UV 215 nm wasmonitored. Before injection of samples the column was equilibrated untila stable baseline was achieved. Samples were diluted to a concentrationof 1 mg/mL using mobile phase and a 30 μL volume was injected. Tomonitor column performance. BioRad (Hercules, Calif.) gel filtrationstandards were used.

Purification results are presented in Table 6. In particular, Ab-Bproduct as well as low molecular weight (LMW), aggregate andglycovariant (GV) impurities were monitored after Protein-A allinitychromatography, CHT hydroxyapatite mixed mode chromatography, Phenyl HPhydrophobic interaction chromatography. With every stage of thepurification process, there were increasingly reduced levels (%) of eachimpurity that was monitored, resulting in Ab-B product with at least 95%purity.

TABLE 6 Quantitative assessment of Ab-B purity throughout thepurification method. Percentage of aggregate, variant, Ab-B andlow-mobility product-associated variant after Protein-A affinitychromatography, CHT hydroxyapatite mixed mode chromatography, and PhenylHP hydrophobic interaction chromatography is shown for an exemplarypurification preparation of Ab-B. % % % % Low- Aggregate Variant Ab-Amolecular weight Protein A 9.8 14.2 72.3 3.8 CHT 0.0 7.9 87.9 4.2 PhenylHP 0.0 0.0 95.6 4.3

Additional process-related impurity monitoring was performed toquantitate clearance of host cell proteins, residual Protein A, dsDNAand glycans (e.g., ß-D-glucan) as a result of purification methods thatinclude a lectin-binding monitoring step. See, Table 7. Overall, thepurification scheme resulted in reduced levels of impurities in thepurified antibody sample.

TABLE 7 Quantitative assessment of process-related impurity clearanceprovided by the purification methods. The concentration (relative toantibody) of P. pastoris host cell protein (HCP), S. cerevisiae hostcell protein (HCP), residual Protein A, dsDNA and β-D-glucan afterProtein-A affinity chromatography, CHT hydroxyapatite mixed modechromatography, and Phenyl HP hydrophobic interaction chromatography isshown for Ab-B. P. pastoris S. cerevisiae Residual β-D- HCP HCP ProteinA dsDNA glucan ppm ppm ppm ppm ppb Protein A 2,314 126 6.1 2.4 5.8 CHT282 57 <0.4 2.8 2.0 Phenyl HP 21 3.7 <0.4 1.5 7.8

Thus, the chromatographic purification methods demonstrated improvedantibody purity. In particular, the final product had greater than 95%purity following Protein-A affinity chromatography, CHT hydroxyapatitemixed mode chromatography and Phenyl-HP hydrophobic interactionchromatography. In addition, the lectin binding assay performed onprocess intermediates demonstrated that the described purificationprocess led to purified Ab-B with reduced GNA binding activity (see,FIG. 8). The lectin binding assay performed on pools of HIC fractionsdemonstrated that selection of appropriate HIC elution fractions tocombine may lead to a HIC Pool with reduced GNA binding activity, byexclusion of other fractions that have higher GNA binding activity (see,FIG. 9).

Example 4: Ab-C Fab Purification and Recovery

This example demonstrates that the lectin-binding assay disclosed hereinmay be used to detect glycosylation impurities of recombinant antibodyfragments generated in in P. pastoris.

P. pastoris cells containing stably integrated sequences encoding theAb-C Fab were cultured and expression of the antibody fragment wasinduced. Alternatively, the Ab-C Fab can be produced chemically byproteolysis of the full-length Ab-C expressed antibody.

Briefly, clarified culture supernatant was contacted on a mixed moderesin at a low pH and low conductivity, washed, and then eluted with agradient strategy that employed raising the pH and conductivitysimultaneously. Eluted fractions were monitored for quality andappropriate fractions pooled and buffer exchanged into a final buffer.In particular, fractions were monitored for glycosylation impurities(RU) using the GNA lectin assay described above.

Antibody fragment purity was also monitored using size-exclusionchromatography. (SE-HPLC) using an Agilent (Santa Clara. Calif.) 1200Series HPLC with UV detection instrument. For sample separation, aTSKgel GS3000SWx1 7.8×300 mm column connected with a TSKgel Guard SWx16×40 mm from Tosoh Bioscience (King of Prussia, Pa.) was used. A 100 mMsodium phosphate, 200 mM sodium chloride pH 6.5 was used as mobile phasewith a flow rate of 0.5 ml/min in isocratic mode and absorbance at UV215 nm was monitored. Before injection of samples the column wasequilibrated until a stable baseline was achieved. Samples were dilutedto a concentration of 1 mg/mL using mobile phase and a 30 μL volume wasinjected. To monitor column performance, BioRad (Hercules, Calif.) gelfiltration standards were used.

Purification results are presented in Table 8. In particular. Ab-C Fabproduct as well as low molecular weight (LMW), aggregate andglycovariant (GV) impurities were monitored after mixed modechromatography using size-exclusion chromatography. Additionally,glycosylated impurities were detected using the GNA lectin assay. Thepurification resulted in Ab-C Fab product with about 90% purity.

TABLE 8 Quantitative assessment of Ab-C Fab purity throughout thepurification method. Percentage of aggregate, variant, Ab-C Fab andlow-mobility product-associated variant after mixed mode chromatographyis shown for an purification preparation of Ab-C Fab. % % Low- Purified% % Ab-C molecular Protein RU Aggregate Variant Fab weight Ab-C Fab 11.56.8 3.1 89.9 0.2

Thus, the purification methods including chromatography andlectin-monitoring of impurities demonstrated Fab antibody fragmentpurity. In particular, the final product had greater than 90% purityfollowing mixed mode chromatography.

The above description of various illustrated embodiments of theinvention is not intended to be exhaustive or to limit the invention tothe precise form disclosed. While specific embodiments of, and examplesfor, the invention are described herein for illustrative purposes,various equivalent modifications are possible within the scope of theinvention, as those skilled in the relevant art will recognize. Theteachings provided herein of the invention can be applied to otherpurposes, other than the examples described above.

The invention may be practiced in ways other than those particularlydescribed in the foregoing description and examples. Numerousmodifications and variations of the invention are possible in light ofthe above teachings and, therefore, are within the scope of the appendedclaims.

These and other changes can be made to the invention in light of theabove detailed description. In general, in the following claims, theterms used should not be construed to limit the invention to thespecific embodiments disclosed in the specification and the claims.Accordingly, the invention is not limited by the disclosure, but insteadthe scope of the invention is to be determined entirely by the followingclaims.

Certain teachings related to methods for obtaining a clonal populationof antigen-specific B cells were disclosed in U.S. Provisional patentapplication No. 60/801,412, filed May 19, 2006, and U.S. PatentApplication Pub. No. 2012/0141982, the disclosure of each of which isherein incorporated by reference in its entirety.

Certain teachings related to humanization of rabbit-derived monoclonalantibodies and preferred sequence modifications to maintain antigenbinding affinity were disclosed in International Application No.PCT/US2008/064421, corresponding to International Publication No.WO/2008/144757, entitled “Novel Rabbit Antibody Humanization Methods andHumanized Rabbit Antibodies”, filed May 21, 2008, the disclosure ofwhich is herein incorporated by reference in its entirety.

Certain teachings related to producing antibodies or fragments thereofusing mating competent yeast and corresponding methods were disclosed inU.S. patent application Ser. No. 11/429,053, filed May 8, 2006. (U.S.Patent Application Publication No. US2006/0270045), the disclosure ofwhich is herein incorporated by reference in its entirety.

The entire disclosure of each document cited herein (including patents,patent applications, journal articles, abstracts, manuals, books, orother disclosures), including each document cited in the Background.Summary, Detailed Description, and Examples, is hereby incorporated byreference herein in its entirety.

1. A process for purifying a desired recombinant polypeptide from one ormore samples resulting from a fermentation process that comprisesculturing a desired cell or microbe under conditions that result in theexpression and secretion of the recombinant polypeptide and one or moreimpurities into the fermentation medium; wherein the purificationprocess includes detecting the amount and/or type of glycosylatedimpurities in the sample(s) using a lectin that binds to saidglycosylated impurities.
 2. The process of claim 1, wherein: (i) saidprocess further comprises contacting the sample(s) with at least onechromatographic support and separating the desired recombinantpolypeptide, optionally wherein said process further comprises detectingthe amount and/or type of glycosylated impurities in the eluate orfractions thereof using a lectin that binds to said glycosylatedimpurities; (ii) wherein the detection step is effected using at leastone lectin selected from ConA LCH, GNA or GNL, RCA, DC-SIGN, L-SIGN,PNA, AIL, VVL, WGA, SNA, MAL, MAH, UEA and AAL, optionally wherein thelectin is bound to a support; (iii) the detection step uses aprotein-protein interaction monitoring process, optionally wherein theprotein-protein interaction monitoring process uses lightinterferometry, dual polarization interferometry, static lightscattering, dynamic light scattering, multi-angle light scattering,surface plasmon resonance, ELISA, chemiluminescent ELISA, far western,or electroluminescence; (iv) the impurities are the result of O-linkedglycosylation; (v) the glycosylated impurity is a glycovariant of thedesired recombinant polypeptide, further wherein the desired recombinantpolypeptide is a homopolymeric or heteropolymeric polypeptide; (vi) theglycosylated impurity is a glycovariant of the desired recombinantpolypeptide, further wherein the desired recombinant polypeptide is ahomopolymeric or heteropolymeric polypeptide; (vii) the glycosylatedimpurity is a glycovariant of the desired recombinant polypeptide,further wherein the desired recombinant polypeptide is a homopolymericor heteropolymeric polypeptide, further wherein the desired recombinantpolypeptide is a hormone, growth factor, receptor, antibody, cytokine,receptor ligand, transcription factor or enzyme; (viii) the glycosylatedimpurity is a glycovariant of the desired recombinant polypeptide,further wherein the desired recombinant polypeptide is a homopolymericor heteropolymeric polypeptide, further wherein the desired recombinantpolypeptide is a hormone, growth factor, receptor, antibody, cytokine,receptor ligand, transcription factor or enzyme, further wherein thedesired recombinant polypeptide is an antibody or an antibody fragment;(ix) the glycosylated impurity is a glycovariant of the desiredrecombinant polypeptide, further wherein the desired recombinantpolypeptide is a homopolymeric or heteropolymeric polypeptide, furtherwherein the desired recombinant polypeptide is a hormone, growth factor,receptor, antibody, cytokine, receptor ligand, transcription factor orenzyme, further wherein the desired recombinant polypeptide is anantibody or an antibody fragment, further wherein the antibody orantibody fragment is a human antibody or a humanized antibody orfragment thereof; (x) the glycosylated impurity is a glycovariant of thedesired recombinant polypeptide, further wherein the desired recombinantpolypeptide is a homopolymeric or heteropolymeric polypeptide, furtherwherein the desired recombinant polypeptide is a hormone, growth factor,receptor, antibody, cytokine, receptor ligand, transcription factor orenzyme, further wherein the desired recombinant polypeptide is anantibody or an antibody fragment, further wherein the antibody orantibody fragment is a human antibody or a humanized antibody orfragment thereof, optionally wherein said humanized antibody is ofmouse, rat, rabbit, goat, sheep, or cow origin; (xi) the glycosylatedimpurity is a glycovariant of the desired recombinant polypeptide,further wherein the desired recombinant polypeptide is a homopolymericor heteropolymeric polypeptide, further wherein the desired recombinantpolypeptide is a hormone, growth factor, receptor, antibody, cytokine,receptor ligand, transcription factor or enzyme, further wherein thedesired recombinant polypeptide is an antibody or an antibody fragment,further wherein the antibody or antibody fragment is a human antibody ora humanized antibody or fragment thereof, optionally wherein saidhumanized antibody is of rabbit origin; (xii) the glycosylated impurityis a glycovariant of the desired recombinant polypeptide, furtherwherein the desired recombinant polypeptide is a homopolymeric orheteropolymeric polypeptide, further wherein the desired recombinantpolypeptide is a hormone, growth factor, receptor, antibody, cytokine,receptor ligand, transcription factor or enzyme, further wherein thedesired recombinant polypeptide is an antibody or an antibody fragment,further wherein said antibody or antibody fragment comprises amonovalent, bivalent, or multivalent antibody; (xiii) the glycosylatedimpurity is a glycovariant of the desired recombinant polypeptide,further wherein the desired recombinant polypeptide is a homopolymericor heteropolymeric polypeptide, further wherein the desired recombinantpolypeptide is a hormone, growth factor, receptor, antibody, cytokine,receptor ligand, transcription factor or enzyme, further wherein thedesired recombinant polypeptide is an antibody or an antibody fragment,further wherein said antibody or antibody fragment comprises amonovalent, bivalent, or multivalent antibody, further wherein saidantibody or antibody fragment specifically binds to IL-2, IL-4, IL-6,IL-10, IL-12, IL-13, IL-17, IL-18, IFN-alpha, IFN-gamma, BAFF, CXCL13,IP-10, CBP, angiotensin (angiotensin I and angiotensin II), Nav1,7,Nav1,8, VEGF, PDGF, EPO, EGF, FSH, TSH, hCG, CGRP, NGF, TNF, HGF, BMP2,BMP7, PCSK9 or HRG; (xiv) different samples or eluates or fractionsthereof containing the desired recombinant polypeptide are pooled basedon the amount and/or type of detected glycosylated impurity; (xv)different samples or eluates or fractions thereof containing the desiredrecombinant polypeptide are pooled based on the amount and/or type ofdetected glycosylated impurity relative to the amount of recombinantpolypeptide (xvi) certain samples or eluate or fractions thereof arediscarded based on the amount and/or type of detected glycosylatedimpurities; (xvii) certain samples or fractions are treated to reduceand/or remove the glycosylated impurities based on the amount and/ortype of detected glycosylated impurities, optionally wherein saidtreatment includes one or more of (i) addition of an enzyme or otherchemical moiety that removes glycosylation and (ii) removal of theglycosylated impurities by effecting one or more lectin binding steps;(xviii) size exclusion chromatography is effected to monitor impurities,optionally wherein the size exclusion chromatographic support isGS3000SW; (xix) size exclusion chromatography is effected to monitorimpurities, further wherein the size exclusion chromatographic supportis GS3000SW, optionally wherein a buffer comprising 100 mM sodiumphosphate, 200 mM sodium chloride pH 6.5 is applied to thechromatographic support to elute the desired recombinant polypeptide;(xx) the host cell is a yeast or filamentous fungi; (xxi) the host cellis a yeast or filamentous fungi, further wherein the yeast is selectedfrom Arxiozyma; Ascobotryozyma; Citeromyces; Debaryomyces; Dekkera;Eremothecium; Issatchenkia; Kazachstania; Kluyveromyces; Kodamaea;Lodderomyces; Pachysolen; Pichia; Saccharomyces; Saturnispora;Tetrapisispora; Torulaspora; Williopsis; Zygosaccharomyces; Yarrowia;Rhodosporidium; Candida; Hansenula; Filobasium; Sporidiobolus; Bullera;Leucosporidium and Filobasidella; (xxii) the host cell is a yeast orfilamentous fungi, further wherein the yeast is selected from Arxiozyma;Ascobotryozyma; Citeromyces; Debaryomyces; Dekkera; Eremothecium;Issatchenkia; Kazachstania; Kluyveromyces; Kodamaea; Lodderomyces;Pachysolen; Pichia; Saccharomyces; Saturnispora; Tetrapisispora;Torulaspora; Williopsis; Zygosaccharomyces; Yarrowia; Rhodosporidium;Candida; Hansenula; Filobasium; Sporidiobolus; Bullera; Leucosporidiumand Filobasidella; optionally wherein the yeast is Pichia pastoris,Pichia angusta, Pichia guillermordii, Pichia methanolica or Pichiainositovera; (xxiii) the host cell is a yeast or filamentous fungi,further wherein the yeast is selected from Arxiozyma; Ascobotryozyma;Citeromyces; Debaryomyces; Dekkera; Eremothecium; Issatchenkia;Kazachstania; Kluyveromyces; Kodamaea; Lodderomyces; Pachysolen; Pichia;Saccharomyces; Saturnispora; Tetrapisispora; Torulaspora; Williopsis;Zygosaccharomyces; Yarrowia; Rhodosporidium; Candida; Hansenula;Filobasium; Sporidiobolus; Bullera; Leucosporidium and Filobasidella;further wherein the yeast is Pichia pastoris, Pichia angusta, Pichiaguillermordii, Pichia methanolica or Pichia inositovera; optionallywherein the yeast is Pichia pastoris; (xxiv) the host cell is a yeast orfilamentous fungi, further wherein the yeast is selected from Arxiozyma;Ascobotryozyma; Citeromyces; Debaryomyces; Dekkera; Eremothecium;Issatchenkia; Kazachstania; Kluyveromyces; Kodamaea; Lodderomyces;Pachysolen; Pichia; Saccharomyces; Saturnispora; Tetrapisispora;Torulaspora; Williopsis; Zygosaccharomyces; Yarrowia; Rhodosporidium;Candida; Hansenula; Filobasium; Sporidiobolus; Bullera; Leucosporidiumand Filobasidella; further wherein the yeast is Pichia pastoris, Pichiaangusta, Pichia guillermordii, Pichia methanolica or Pichia inositovera;further wherein the yeast is Pichia pastoris; optionally wherein thePichia pastoris expresses an antibody or antibody fragment; and/or (xxv)the host cell is a yeast or filamentous fungi, optionally wherein thefilamentous fungi is selected from Aspergillus, Trichoderma,Penicillium, Rhizopus, Paecilomyces, Fusarium, Neurospora and Claviceps.3-17. (canceled)
 18. The process of claim 2, embodiment (vi), whereinthe chromatographic purification of the desired recombinant polypeptidecomprises; (a) contacting the sample(s) with an affinity chromatographicsupport and separating the desired recombinant polypeptide from thesupport; (b) contacting the eluate or fraction thereof of step (a) witha mixed mode chromatographic support and selectively eluting the desiredrecombinant polypeptide from the support; and (c) contacting the eluateor fraction thereof of step (b) with a hydrophobic interactionchromatographic support and selectively eluting the desired recombinantpolypeptide from the support, wherein the eluate or fraction thereof ofstep (c) comprises substantially purified desired recombinantpolypeptide,
 19. The process of claim 18, wherein: (i) the eluate orfraction thereof from at least one of step (a), step (b) and step (c) iscontacted with the lectin to detect the amount and/or type ofglycosylated impurities in the eluate or fraction thereof; (ii) theeluate of step (c) comprises less than 50 ng/mg (5%) of glycovariant;(iii) the eluate of step (c) comprises less than 25 ng/mg ofglycovariant; (iv) the eluate of step (c) comprises less than 10 ng/mgof glycovariant; (v) the eluate of step (c) comprises lectin activityranging from about 0.2 to about 2 RU as measured by a lectin bindingkinetic assay; (vi) the eluate of step (c) comprises less than 10 ng/mg(10 ppm) of fungal cell protein; (vii) the eluate of step (c) comprisesless than 5 ng/mg of a fungal cell protein; (viii) the eluate of step(c) comprises less than 2 ng/mg of a fungal cell protein; (ix) theeluate of step (c) comprises less than 10 ng/mg of nucleic acid; (x) theeluate of step (c) comprises less than 5 ng/mg of nucleic acid; (xi) theaffinity chromatographic support comprises an immunoaffinity ligand,optionally wherein the immunoaffinity ligand is Protein A; (xii) theaffinity chromatographic support comprises an immunoaffinity ligand,optionally wherein the immunoaffinity ligand is lectin; (xiii) the mixedmode chromatographic support is selected from ceramic hydroxyapatite,ceramic fluoroapatite, crystalline hydroxyapatite, crystallinefluoroapatite, CaptoAdhere, Capto MMC, HEA Hypercel, PPA Hypercel andToyopearl MX-Trp-650M, optionally wherein the mixed mode chromatographicsupport is ceramic hydroxyapatite; (xiv) the hydrophobic interactionchromatographic support is selected from Butyl Sepharose 4 FF, Butyl-SSepharose FF, Octyl Sepharose 4 FF, Phenyl Sepharose BB, PhenylSepharose HP, Phenyl Sepharose 6 FF High Sub, Phenyl Sepharose 6 FF LowSub, Source 1 SETH, Source 15ISO, Source 15PHE, Capto Phenyl, CaptoButyl, Streamline Phenyl, TSK Ether 5PW (20 um and 30 um), TSK Phenyl5PW (20 um and 30 um), Phenyl 650S, M, and C, Butyl 650S, M and C,Hexyl-650M and C, Ether-650S and M, Butyl-600M, Super Butyl-550C,Phenyl-600M, PPG-600M; YMC-Pack Octyl Columns-3, 5, 10P, 15 and 25 umwith pore sizes 120, 200, 300 A, YMC-Pack Phenyl Columns-3, 5, 10P, 15and 25 um with pore sizes 120, 200 and 300 A, YMC-Pack Butyl Columns-3,5, 10P, 15 and 25 um with pore sizes 120, 200 and 300 A, CellufineButyl, Cellufine Octyl, Cellufine Phenyl; WP HI-Propyl (C3); Macroprept-Butyl or Macroprep methyl; and High Density Phenyl-HP2 20 um,optionally wherein the hydrophobic interaction chromatographic supportis polypropylene glycol (PPG) 600M or Phenyl Sepharose HP; (xv) theaffinity chromatographic support comprises an immunoaffinity ligand,further wherein the immunoaffinity ligand is Protein A, optionallywherein a buffer comprising about 1 M arginine, pH 4.0 is applied to thechromatographic support to elute the desired multi-subunit complex;(xvi) the mixed mode chromatographic support is selected from ceramichydroxyapatite, ceramic fluoroapatite, crystalline hydroxyapatite,crystalline fluoroapatite, CaptoAdhere, Capto MMC, HEA Hypercel, PPAHypercel and Toyopearl MX-Trp-650M, further wherein the mixed modechromatographic support is ceramic hydroxyapatite, optionally wherein abuffer comprising (i) about 5 mM sodium phosphate, pH 6,5, and about 0 Mto about 1.5 M sodium chloride, or (ii) about 5 mM to 0.25 M sodiumphosphate, pH 6,5, is applied to the chromatographic support to elutethe desired recombinant polypeptide; and/or (xvii) the hydrophobicinteraction chromatographic support is selected from Butyl Sepharose 4FF, Butyl-S Sepharose FF, Octyl Sepharose 4 FF, Phenyl Sepharose BB,Phenyl Sepharose HP, Phenyl Sepharose 6 FF High Sub, Phenyl Sepharose 6FF Low Sub, Source 1 SETH, Source 15ISO, Source 15PHE, Capto Phenyl,Capto Butyl, Streamline Phenyl, TSK Ether 5PW (20 um and 30 um), TSKPhenyl 5PW (20 um and 30 um), Phenyl 650S, M, and C, Butyl 650S, M andC, Hexyl-650M and C, Ether-650S and M, Butyl-600M, Super Butyl-550C,Phenyl-600M, PPG-600M; YMC-Pack Octyl Columns-3, 5, 10P, 15 and 25 umwith pore sizes 120, 200, 300A, YMC-Pack Phenyl Columns-3, 5, 10P, 15and 25 um with pore sizes 120, 200 and 300A, YMC-Pack Butyl Columns-3,5, 10P, 15 and 25 um with pore sizes 120, 200 and 300A, Cellufine Butyl,Cellufine Octyl, Cellufine Phenyl; WP HI-Propyl (C3); Macroprep t-Butylor Macroprep methyl; and High Density Phenyl-HP2 20 um, further whereinthe hydrophobic interaction chromatographic support is polypropyleneglycol (PPG) 600M or Phenyl Sepharose HP, optionally wherein a buffercomprising about 0.7 M to 0 M sodium sulfate in 20 mM sodium phosphate,DH 7.0 is applied to the chromatographic support to elute the desiredrecombinant polypeptide. 20-21. (canceled)
 22. The process of claim 2,embodiment (xiv), wherein: (i) samples or eluate or fractions thereofcomprising less than 10% glycovariant are pooled; (ii) samples or eluateor fractions thereof comprising less than 5% glycovariant are pooled;(iii) samples or eluate or fractions thereof comprising less than 1%glycovariant are pooled; (iv) samples or eluate or fractions thereofcomprising less than 0.5% glycovariant are pooled; (v) said processfurther comprises pooling different samples or eluate or fractionsthereof based on the purity of the desired recombinant polypeptide,optionally wherein the purity is determined by measuring the mass ofglycosylated heavy chain polypeptide and/or glycosylated light chainpolypeptide as a percentage of total mass of heavy chain polypeptideand/or light chain polypeptide; (vi) said process further comprisespooling different samples or eluate or fractions thereof based on thepurity of the desired recombinant polypeptide, wherein samples or eluateor fractions thereof comprising greater than 91% purity are pooled,optionally wherein the purity is determined by measuring the mass ofglycosylated heavy chain polypeptide and/or glycosylated light chainpolypeptide as a percentage of total mass of heavy chain polypeptideand/or light chain polypeptide; (vii) said process further comprisespooling different samples or eluate or fractions thereof based on thepurity of the desired recombinant polypeptide, wherein samples or eluateor fractions thereof comprising greater than 97% purity are pooled,optionally wherein the purity is determined by measuring the mass ofglycosylated heavy chain polypeptide and/or glycosylated light chainpolypeptide as a percentage of total mass of heavy chain polypeptideand/or light chain polypeptide; and/or (viii) said process furthercomprises pooling different samples or eluate or fractions thereof basedon the purity of the desired recombinant polypeptide, wherein samples oreluate or fractions thereof comprising greater than 99% purity arepooled, optionally wherein the purity is determined by measuring themass of glycosylated heavy chain polypeptide and/or glycosylated lightchain polypeptide as a percentage of total mass of heavy chainpolypeptide and/or light chain polypeptide.
 23. The process of claim 2,embodiment (xiv), wherein: (i) samples or eluate or fractions thereofcomprising less than 5% glycovariant are pooled; (ii) samples or eluateor fractions thereof comprising less than 10% glycovariant are pooled;(iii) samples or eluate or fractions thereof comprising less than 1%glycovariant are pooled; (iv) samples or eluate or fractions thereofcomprising less than 0.5% glycovariant are pooled; (v) said processfurther comprises pooling different samples or eluate or fractionsthereof based on the purity of the desired recombinant polypeptide,optionally wherein the purity is determined by measuring the mass ofglycosylated heavy chain polypeptide and/or glycosylated light chainpolypeptide as a percentage of total mass of heavy chain polypeptideand/or light chain polypeptide; (vi) said process further comprisespooling different samples or eluate or fractions thereof based on thepurity of the desired recombinant polypeptide, wherein samples or eluateor fractions thereof comprising greater than 91% purity are pooled,optionally wherein the purity is determined by measuring the mass ofglycosylated heavy chain polypeptide and/or glycosylated light chainpolypeptide as a percentage of total mass of heavy chain polypeptideand/or light chain polypeptide; (vii) said process further comprisespooling different samples or eluate or fractions thereof based on thepurity of the desired recombinant polypeptide, wherein samples or eluateor fractions thereof comprising greater than 97% purity are pooled,optionally wherein the purity is determined by measuring the mass ofglycosylated heavy chain polypeptide and/or glycosylated light chainpolypeptide as a percentage of total mass of heavy chain polypeptideand/or light chain polypeptide; and/or (viii) said process furthercomprises pooling different samples or eluate or fractions thereof basedon the purity of the desired recombinant polypeptide, wherein samples oreluate or fractions thereof comprising greater than 99% purity arepooled, optionally wherein the purity is determined by measuring themass of glycosylated heavy chain polypeptide and/or glycosylated lightchain polypeptide as a percentage of total mass of heavy chainpolypeptide and/or light chain polypeptide. 24-61. (canceled)
 62. Aprocess for purifying a desired recombinant polypeptide expressed in afungal cell from a mixture comprising the desired polypeptide and atleast one glycosylated impurity, the purification process comprising:(a) contacting the mixture with an affinity chromatographic support andseparating the multi-subunit protein from the support; (b) contactingthe eluate or a fraction thereof of step (a) with a mixed modechromatographic support and selectively eluting the multi-subunitprotein from the support; and (c) contacting the eluate or a fractionthereof of step (b) with a hydrophobic interaction chromatographicsupport and selectively eluting the multi-subunit protein from thesupport, wherein the eluate or a fraction thereof of step (c) comprisessubstantially purified desired recombinant polypeptide; wherein theamount and/or type of glycosylated impurities in the eluate or afraction thereof of step (b) and/or step (c) is detected using a lectinthat binds to said glycosylated impurities and one or more fractions ofthe eluate of step (b) and/or step (c) is selected for furtherprocessing based on the detected amount and/or type of glycosylatedimpurities.
 63. The process of claim 62, wherein: (i) the affinitychromatographic support is a Protein A column; (ii) the affinitychromatographic support is a lectin column; (iii) the mixed modechromatographic support is a hydroxyapatite column; (iv) the hydrophobicinteraction chromatographic support is a PPG-600M column; (v) thedesired recombinant polypeptide is a multi-subunit protein, optionallywherein the multi-subunit protein is an antibody; (vi) the detectionstep is effected using at least one lectin selected from ConA, LCH, GNAor GNL, RCA, DC-SIGN, L-SIGN, PNA, AIL, VVL, WGA, SNA, MAL, MAH, UEA andAAL; (vii) the detection step uses a protein-protein interactionmonitoring process selected from light interferometry, dual polarizationinterferometry, static light scattering, dynamic light scattering,multi-angle light scattering, surface plasmon resonance, ELISA,chemiluminescent ELISA, far western, or electroluminescence, optionallywherein the detection step is effected using GNA and/or DC-SIGNlectin(s) in a light interferometry assay; and/or (viii) the fungal cellis Pichia pastoris. 64-72. (canceled)
 73. A fermentation process forproducing a desired recombinant polypeptide and purifying the desiredrecombinant polypeptide from the fermentation medium, wherein theprocess includes: (i) culturing a host cell or microbe under conditionsthat result in the expression and secretion of the recombinantpolypeptide and one or more impurities into the fermentation medium;(ii) periodically obtaining one or more samples of the fermentationmedium as the fermentation process proceeds or after differentfermentation runs are conducted; (iii) detecting the amount and/or typeof glycosylated impurities in the sample(s) using a lectin that binds tosaid glycosylated impurities, and (iv) based on the amount of detectedglycosylated impurities in the sample(s) modifying one or more of theoperating parameters or conditions of the fermentation process.
 74. Theprocess of claim 73, wherein: (i) the impurities are the result ofO-linked glycosylation; (ii) the detection step is effected using atleast one lectin selected from ConA, LCH, GNA or GNL, RCA, DC-SIGN,L-SIGN, PNA, AIL, VVL, WGA, SNA, MAL, MAH, UEA and AAL; (iii) thedetection step uses a lectin bound to a support; (iv) the detection stepuses a protein-protein interaction monitoring process, optionallywherein the protein-protein interaction monitoring process uses lightinterferometry, dual polarization interferometry, static lightscattering, dynamic light scattering, multi-angle light scattering,surface plasmon resonance, ELISA, chemiluminescent ELISA, far western,or electroluminescence; (v) based on the amount of glycosylatedimpurities detected one or more of the following parameters orconditions of the fermentation process are altered; temperature, pH, gasconstituent, feed constituent, agitation, aeration, antifoam andduration; (vi) the glycosylated impurity is a glycovariant of therecombinant polypeptide; (vii) the recombinant polypeptide is ahomopolymeric or heteropolymeric polypeptide; (viii) the recombinantpolypeptide is a hormone, growth factor, receptor, antibody, cytokine,receptor ligand, transcription factor or enzyme; (ix) the recombinantpolypeptide is an antibody or antibody fragment; (x) the host cell is ayeast or filamentous fungi; (xi) the yeast host cell is selected fromArxiozyma; Ascobotrvozyma; Citeromyces; Debaryomyces; Dekkera;Eremothecium; Issatchenkia; Kazachstania; Kluyveromyces; Kodamaea;Lodderomyces; Pachysolen; Pichia; Saccharomyces; Saturnispora;Tetrapisispora; Torulaspora; Williopsis; Zygosaccharomyces; Yarrowia;Rhodosporidium; Candida; Hansenula; Filobasium; Sporidiobolus; Bullera;Leucosporidium and Filobasidella; (xii) the filamentous fungal host cellis selected from Aspergillus, Trichoderma, Penicillium, Rhizopus,Paecilomyces, Fusarium, Neurospora and Claviceps; (xiii) the yeast hostcell is Pichia pastoris, Pichia angusta, Pichia guillermordii, Pichiamethanolica, or Pichia inositovera; (xiv) the yeast host cell is Pichiapastoris, optionally wherein the Pichia pastoris expresses an antibodyor antibody fragment; (xv) wherein said process further includesrecovering or purifying the recombinant polypeptide from thefermentation medium; (xvi) wherein said process further includesrecovering or purifying the recombinant polypeptide from thefermentation medium, further wherein the purification process furthercomprises contacting the sample(s) with at least one chromatographicsupport and selectively eluting the desired recombinant polypeptide;(xvii) wherein said process further comprises detecting the amount ofaggregated and/or disaggregated impurities in the samples or fractionsusing size exclusion chromatography, optionally wherein wherein based onthe amount of aggregated and/or disaggregated impurities detected one ormore of the following parameters or conditions of the fermentationprocess are altered; temperature, pH, gas constituent, feed constituent,agitation, aeration, antifoam and duration; (xviii) the recombinantpolypeptide is an antibody or antibody fragment, further wherein theantibody or antibody fragment is a human antibody or a humanizedantibody or fragment thereof; (xix) the recombinant polypeptide is anantibody or antibody fragment, further wherein the antibody or antibodyfragment is a human antibody or a humanized antibody or fragmentthereof, optionally wherein said humanized antibody is of mouse, rat,rabbit, goat, sheep, or cow origin; (xx) the recombinant polypeptide isan antibody or antibody fragment, further wherein the antibody orantibody fragment is a human antibody or a humanized antibody orfragment thereof, optionally wherein said humanized antibody is ofrabbit origin; (xxi) the recombinant polypeptide is an antibody orantibody fragment, further wherein said antibody or antibody fragmentcomprises a monovalent, bivalent, or multivalent antibody; and/or (xxii)the recombinant polypeptide is an antibody or antibody fragment, furtherwherein said antibody or antibody fragment specifically binds to IL-2,IL-4, IL-6, IL-10, IL-12, IL-13, IL-17, IL-18, IFN-alpha, IFN-gamma,BAFF, CXCL13, IP-10, CBP, angiotensin (angiotensin I and angiotensinII), Nav1,7, Nav1,8, VEGF, PDGF, EPO, EGF, FSH TSH, hCG, CGRP, NGF, TNF,HGF, BMP2, BMP7, PCSK9 or HRG. 75-91. (canceled)
 92. The process ofclaim 74, embodiment (xv), wherein: (i) the purification process furthercomprises pooling different samples or eluates or fractions thereofcontaining the desired recombinant polypeptide based on the amountand/or type of detected glycosylated impurity; and/or (ii) thepurification process further comprises pooling different samples oreluates or fractions thereof containing the desired recombinantpolypeptide based on the amount and/or type of detected glycosylatedimpurity relative to the amount of recombinant polypeptide,
 93. Theprocess of claim 74, embodiment (xvi), wherein: (i) the purificationprocess further comprises pooling different samples or eluates orfractions thereof containing the desired recombinant polypeptide basedon the amount and/or type of detected glycosylated impurity relative tothe amount of recombinant polypeptide; and/or (ii) the purificationprocess further comprises pooling different samples or eluates orfractions thereof containing the desired recombinant polypeptide basedon the amount and/or type of detected glycosylated impurity. 94-100.(canceled)